CN104804787B - Methanation method and device for preparing synthetic natural gas - Google Patents
Methanation method and device for preparing synthetic natural gas Download PDFInfo
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Abstract
Disclosure of the inventionA methanation method for preparing synthetic natural gas features that the raw gas purified to remove catalyst poison is fed to a first-stage methanation reactor to obtain most of H 2 And the reaction gas is subjected to methanation reaction with CO, and the reaction gas enters a second-stage methanation reactor to complete the methanation reaction of the rest carbon oxide and hydrogen, so that CH in the methanated dry gas is obtained 4 Greater than 93% of heat value>33MJ／M 3 . The invention also discloses a device for realizing the method. The invention is a high-efficiency energy-saving compact large-scale methanation process technology and device for preparing natural gas, is particularly suitable for the situation that coal gasification and coal gas purification of a plurality of synthetic ammonia plants are low-pressure devices and synthetic ammonia is medium-high pressure devices, can be transformed into a synthetic artificial natural gas device by utilizing high-pressure compressors and high-pressure synthesis devices of medium and small ammonia plants in China, saves a large amount of investment, and has very important function.
Description
Technical Field
The invention relates to the technical field of chemical engineering, in particular to a methanation method and a methanation device for preparing synthetic natural gas.
Background
At present, the process for preparing natural gas from foreign coal comprises the steps of firstly preparing synthetic gas from coal gasification and then cracking the synthetic gas through CO conversion to prepare the synthetic gas
The raw synthesis gas is methanated to natural gas, wherein the key technology of methanation adopts high-temperature adiabatic methanation, such as TREMP of Tops phi e company TM The process (Zhuruichun and the like, research on coal-to-natural gas process technology, No. 17 No. 6 in 2011, P81-85) as shown in figure 4, adopts five high-temperature adiabatic reactors for series reaction, and is similar to other methanation technologies such as Lurgi and DAVY. Therefore, the process flow is long, the equipment is more, the investment is large, and the energy consumption is high.
Currently with a hydrogen-containing radical 2 、CO、CO 2 The methanation of artificial natural gas prepared by methanation is characterized in that the raw material gas is different, although the pressure is different (for example, the natural gas prepared by coke oven is about 1MPa, and the methane prepared by coal synthesis gas is about 3MPa for methanation introduced by Datang), the methanation process is basically a front pressure grade and a back pressure grade, the pressure of the raw material gas is lower, the methanation is carried out without pressurization, the low-pressure methanation reaction is easy to control, the power consumption of a compressor is reduced, the equipment is huge under the low pressure condition, for example, a natural gas device which produces 40 billion of parts per year is divided into three periods, A, B two sets of devices are arranged for producing 13 billion of parts per year in the first period, more than 100 methanation equipment with 40 billion of parts can be formed, and the product day is a productThe pipe network gas supply for natural gas is to reduce the gas transmission pipe diameter, the design in China is mostly 10MPa and also 12MPa, namely, the product natural gas after methanation needs to be compressed to 10MPa again, dehydrated at 40 ℃, then dehydrated by water and further dehydrated and dried by triethylene glycol, so as to ensure that the dew point of the gas is-3 ℃, and the pressure of the prepared compressed natural gas is higher than 20 MPa. Since the methanation reaction is a volume reduction reaction, the methanation reaction is represented by the following reaction formula:
CO+3H 2 =CH 4 +H 2 O
CO 2 +4H 2 =CH 4 +2H 2 O
the CH in the product can be seen 4 Balance content
The pressure P is increased, the equilibrium content of methanation in the reaction product is greatly increased, the reaction speed of methanation is increased under high pressure, so that the space velocity of methanation is increased, and the space velocity V under pressure is increased p =V s P n Wherein V is the space velocity under normal pressure, and n is about 0.4.
Disclosure of Invention
In order to overcome the defects in the prior art, the application provides a high-efficiency, energy-saving and compact large-scale natural gas preparation process technology and device through methanation, and particularly aims at the situation that coal gasification and coal gas purification of a plurality of synthetic ammonia plants are low-pressure devices and synthetic ammonia is medium-high pressure devices, wherein a plurality of devices for medium-low pressure methanol coproduction are arranged, so that the investment can be fully reduced by utilizing original equipment, and the device has a very important function.
In order to achieve the purpose, the invention adopts the following technical scheme:
a methanation method for preparing synthetic natural gas features that the raw gas without catalyst poison is first treated in a methanation reactor under the pressure of gasifying and purifying to obtain most of H 2 And methanation of CO>0.5 percent of the reaction gas enters a second-stage methanation reactor to complete the methanation reaction of the rest carbon oxide and hydrogen, so as to obtain CH in the dry gas after methanation 4 >93% heat value>33MJ／M 3 (ii) a The first-stage methanation reactionThe device is a water-cooling or heat-conducting oil heat-exchange byproduct steam methanation reactor, and the second-stage methanation reactor is a heat-exchange methanation reactor or an adiabatic methanation reactor
The water-cooling or heat-conducting oil byproduct steam methanation reactor is a wound tube type water-cooling or heat-conducting oil heat exchange byproduct steam methanation reactor.
The raw material gas is coal gasification synthesis gas, the mole percentage of CO in the raw material gas is 10-30%, the raw material gas is subjected to deep purification and heat exchange heating, part of the raw material gas and circulating gas are mixed and enter a first-stage methanation reactor for reaction, the reaction gas which is discharged from the first-stage methanation reactor is mixed with the rest raw material gas and then enters a second-stage methanation reactor, the reaction gas which is discharged from the second-stage methanation reactor is cooled, separated, partially subjected to pressure rise by a circulator and used as circulating gas to be converged with part of the synthesis gas which enters the first-stage methanation reactor, and the rest of the reaction gas is used as synthesis natural gas product gas.
The reaction pressure of the first-stage methanation reactor is 2-6 MPa.
The reaction pressure of the two-stage methanation reactor is improved by 1-30MPa compared with the reaction pressure of the first-stage methanation reactor.
The utility model provides a methanation assembly for making synthetic natural gas as above, is including one section methanation reactor and two-stage process methanation reactor that connect gradually, one section methanation reactor external drum byproduct steam, one section methanation reactor be water-cooling or heat conduction oil heat transfer byproduct steam methanation reactor, two-stage process methanation reactor be heat transfer methanation reactor or adiabatic methanation reactor.
The water-cooling or heat-conducting oil byproduct steam methanation reactor is a wound pipe type heat-conducting oil heat exchange byproduct steam methanation reactor after water cooling.
The device still include first heat exchanger, second heat exchanger, water cooler, circulator and first water separator, one section methanation reactor, two-stage section methanation reactor, first heat exchanger, second heat exchanger, water cooler, first water separator, circulator connect gradually, the export of circulator and second heat exchanger, the import of one section methanation reactor connect gradually.
The device still include clarifier, first heat exchanger, second heat exchanger, third heat exchanger, water cooler, circulating compressor, first water separator and second water separator, one section methanation reactor, first heat exchanger, first water separator, circulating compressor connect gradually, the export of clarifier and first heat exchanger, one section methanation reactor's import connect gradually, circulating compressor's compressed gas export and second heat exchanger, two sections methanation reactor connect gradually, two sections methanation reactor's export and second heat exchanger, third heat exchanger, water cooler, second water separator connect gradually, circulating compressor's circulating gas export and one section methanation reactor's access connection, the third heat exchanger be connected with the clarifier.
The first-stage methanation reactor comprises two reactors: the device comprises a first methanation reactor, a second methanation reactor, a steam pocket and a water pump, and further comprises a purifier, a first heat exchanger, a second heat exchanger, a third heat exchanger, a water cooler, a first water separator, a second water separator and a circulating compressor, wherein the purifier is connected with the first heat exchanger, the outlet of the first heat exchanger is divided into two paths which are respectively connected with the inlets of the first methanation reactor and the second methanation reactor, the outlet of the first methanation reactor is sequentially connected with the first heat exchanger, the first water separator, the circulating compressor, the second water separator, the third heat exchanger and the second methanation reactor, the outlet of the second methanation reactor is sequentially connected with the third heat exchanger, the water cooler and the second water separator, the circulating gas outlet of the circulating compressor is connected with the inlet of the first methanation reactor, and the outlet of the first-section second methanation reactor is sequentially connected with the second heat exchanger and the circulating compressor.
The invention has the following beneficial effects:
1. the technology of introducing DAVY, Lurgi and Tops phi e high-temperature adiabatic methanation to prepare natural gas at abroad, which is established and established at present, is changed, and methanation reaction, heat exchange and byproduct steam are combined, so that the flow is simplified greatly, equipment is reduced, investment is saved, energy efficiency is improved, cost is reduced, and benefit is improved.
2. High efficiency, high pressure in later period, high synthesis rate and low catalytic amount.
3. The energy is saved, the effect of separating the by-product water is improved under high pressure, and the high-pressure requirement of compressed natural gas production or pipe network conveying is met.
4. The device is beneficial to large-scale device and improves the capability of synthesizing natural gas by a single-line device.
5. The device for synthesizing the artificial natural gas can be reconstructed by utilizing high-pressure compressors and high-pressure synthesis devices of small and medium ammonia plants in China, so that a large amount of investment is saved.
Drawings
FIG. 1 is a schematic block diagram of the principle flow of the method of the present invention.
FIG. 2 is a schematic block diagram of one embodiment of the method of the present invention.
FIG. 3 is a schematic block diagram of another embodiment of the process of the present invention, which includes primary and secondary heat exchanges.
FIG. 4 is a schematic view of an embodiment of the apparatus of the present invention.
FIG. 5 is a schematic diagram of another embodiment of the apparatus of the present invention, in which there are two heat exchangers.
FIG. 6 is a schematic representation of another embodiment of the apparatus of the present invention in which there are three heat exchangers and two water separators.
FIG. 7 is a schematic diagram of another embodiment of the apparatus of the present invention, in which there are two primary methanation reactors.
Fig. 8 is a schematic diagram of a process flow of co-production of methanol from raw synthetic ammonia in embodiment 5 of the present invention.
Fig. 9 is a schematic diagram of the modified synthetic natural gas peak shaving process in example 5 of the present invention.
Description of reference numerals:
1-first-stage methanation reactor, 2-circulating compressor and 3-second-stage methanation reactor
4-steam drum 5-purifier 6-first water separator
7-second water separator 8-first heat exchanger 9-second heat exchanger
10-third heat exchanger 11-water cooler 12-third water separator
1 a-first methanation reactor 1 b-first methanation reactor 13-circulator
14-steam generator
Detailed Description
The invention is described in detail below with reference to the figures and examples.
Example 1
The methanation basic device for preparing the synthetic natural gas as shown in fig. 4 comprises a first-stage methanation reactor 1, a circulating compressor 2, a second-stage methanation reactor 3, a water cooler 11 and a first water separator 6 which are connected in sequence, wherein the first-stage methanation reactor 1 is externally connected with a steam drum 4 to generate by-product steam, the first-stage methanation reactor 1 is a heat exchange type reactor with a winding pipe, and the second-stage methanation reactor 3 is an adiabatic type reactor.
In the embodiment, the pressure of the first-stage methanation synthesis is 3-6 MPa, the pressure of the second-stage methanation synthesis is 10MPa, and the pressure of the second-stage methanation reactor 3 is higher than that of the first-stage methanation reactor 1.
When the device is operated, the purified feed gas is firstly subjected to coal gasification and purification under the pressure grade (for example, 3-6 MPa) and the pressure of the purified feed gas is equal to that of the byproduct steam in the first-stage methanation reactor 1 to carry out most of H 2 And performing methanation reaction on the reaction gas and CO at the reaction temperature of 250-500 ℃, then feeding the reaction gas into a circulating compressor 2 for circulation and pressurization, mixing part of the reaction gas from an outlet of a circulation section with the gas fed into a first-stage methanation reactor 1 to reduce the content of CO in the gas, compressing the rest of the gas to 10MPa, and feeding the compressed gas into a second-stage methanation reactor 3 to complete the methanation reaction of the rest of carbon oxide and hydrogen to obtain CH in the dry gas after methanation 4 >93% heat value>33MJ／M 3 And finally, the reaction gas sequentially passes through a water cooler 11 and a first water separator 6 to obtain SNG.
Example 2
Fig. 5 shows a methanation device for producing synthetic natural gas, which comprises a first section of methanation reactor 1, a second section of methanation reactor 3, a first heat exchanger 8, a second heat exchanger 9, a water cooler 11, a circulator 13 and a first water separator 6, wherein the first section of methanation reactor 1, the second section of methanation reactor 3, the first heat exchanger 8, the second heat exchanger 9, the water cooler 11, the first water separator 6 and the circulator 13 are connected in sequence, and an outlet of the circulator 13 is connected in sequence with an inlet of the second heat exchanger 9 and the first section of methanation reactor 1.
When the device is operated, the purified raw gas is subjected to heat exchange with the reaction gas through the first heat exchanger 8 and is heated to 250-300 ℃, then the raw gas is divided into two strands, one strand of the raw gas enters the first-stage methanation reactor 1 and reacts at about 400 ℃, the reaction gas discharged from the first-stage methanation reactor 1 enters the second-stage methanation reactor 3, the reaction gas discharged from the second-stage methanation reactor 3 is sequentially cooled to 40 ℃ through the first heat exchanger 8, the second heat exchanger 9 and the water cooler 11, and finally, after moisture is separated in the first water separator 6, one part of the reaction gas is used as synthesis product gas, and the other part of the reaction gas is used as circulating gas to be mixed with the raw gas entering the first-stage methanation reactor 1 to synthesize methane. Example 3
The device shown in fig. 6 comprises a purifier 5, a first-stage methanation reactor 1, a second-stage methanation reactor 3, a first heat exchanger 8, a second heat exchanger 9, a third heat exchanger 10, a water cooler 11, a first water separator 6, a second water separator 7 and a steam generator 14, wherein the first-stage methanation reactor 1, the first heat exchanger 8, the first water separator 6, a circulating compressor 2 consisting of a circulating section and a compression section, the second heat exchanger 9 and the second-stage methanation reactor 3 are sequentially connected, an outlet of the second-stage methanation reactor 3 is sequentially connected with the second heat exchanger 9, the third heat exchanger 10, the water cooler 11 and the second water separator 7, and an outlet pipeline of the compression section of the circulating compressor 2 is connected with the second heat exchanger 9 and then connected with an inlet of the high-pressure methanation reactor 3; an outlet pipeline of the struggle reactor 5 firstly passes through the first heat exchanger 8 and then is converged with an outlet pipeline of a circulation section of the circulating compressor 2 and then is connected with an inlet of the first section of the methanation reactor 1. The first-stage methanation reactor 1 is externally connected with a steam generator 14, and heat conduction oil is used for heat exchange to produce steam as a byproduct in the steam generator 14.
When the device is operated, a raw material gas with the pressure of 3-6 MPa is heated by the reaction gas through the third heat exchanger 10 and then is subjected to deep purification at the temperature of 210 ℃ and above through the purifier 5, then the raw material gas exchanges heat with the reaction gas out of the first-section methanation reactor 1 through the first heat exchanger 8, is heated to the temperature of 250 ℃ and above, and then is converged with the circulation gas to enter the first-section methanation reactor 1 to carry out most of H 2 And the reaction heat is taken out by the gasification and heat absorption of heat conducting oil in the pipe through methanation reaction of CO, the first-section methanation reactor 1 is externally connected with a steam generator 14, the heat conducting oil is adopted in the pipe of the steam generator 14 for heat exchange, and steam is byproduct. And (2) after the reaction gas (with the temperature of about 300-500 ℃) out of the first-stage methanation reactor 1 is subjected to heat exchange and temperature reduction through a first heat exchanger 8, partial water is separated out through a first water separator 6 (at about 40 ℃), the rest of the reaction gas enters a circulating compressor 2, then partial gas is mixed with the raw gas entering the first-stage methanation reactor 1 from an outlet of a circulating section, the rest of the gas is compressed to 12MPa through an outlet of a compression section of the circulating compressor 2 and enters a second heat exchanger 9, the compressed gas is subjected to temperature rise (at about 250 ℃) through the second heat exchanger 9 and then enters a second-stage methanation reactor 3 to complete methanation reaction of the rest of carbon oxide and hydrogen, and the reaction gas out of the second-stage methanation reactor 3 sequentially passes through the second heat exchanger 9, a third heat exchanger 10, a water cooler 11 and a second water separator 7 to obtain SNG. The above device is suitable for using methane-rich gas (CH) as raw material gas 4 >10%) of the reaction conditions.
Example 4
As shown in FIG. 7, when the raw material gas is gasified with coal water slurry or pulverized coal, the composition of CH is 4 Low content of H 2 When CO content is very high, in order to avoid the phenomenon that the reaction is too violent at the beginning of methanation, the first section methanation reactor adopts two: the device comprises a first methanation reactor 1a and a second methanation reactor 1b which are respectively externally connected with a steam drum and a pump, and the device comprises a purifier 5, a first heat exchanger 8, a second heat exchanger 9, a third heat exchanger 10, a water cooler 11, a first water separator 6, a second water separator 7 and a third water separator 12 besides a circulating compressor 2 and a second methanation reactor 3. The outlet pipeline of the purifier 5 is divided into two paths after passing through the first heat exchanger 8, and the two paths are respectively connected with the first methanation reactor 1a and the second methanation reactor 1b, namelyThe first methanation reactor 1a and the second methanation reactor 1b are connected in parallel, the outlet of the first methanation reactor 1a is divided into two paths after passing through a first heat exchanger 8, one path is connected with a pipeline entering the first methanation reactor 1b, the other path is connected with a first water separator 6 and a circulating compressor 2 in sequence, and the outlet of the first methanation reactor 1b is connected with the inlet of the compression section of the circulating compressor 2 after passing through a second heat exchanger 9. The outlet of the circulating compressor 2 is divided into a circulating section outlet and a compressing section outlet, the circulating section outlet is connected with the inlet of the first methanation reactor 1a after passing through the second heat exchanger 9, and the compressing section outlet is connected with the second water separator 7. And the outlet of the second water separator 7 passes through the third heat exchanger 10 and then is sequentially connected with the second-stage methanation reactor 3, the third heat exchanger 10, the water cooler 11 and the third water separator 12.
When the device is operated, the raw gas is deeply purified by the purifier 5 to remove catalyst poison, then is subjected to heat exchange and temperature rise by the reaction gas which is discharged from the first methanation reactor 1a through the first heat exchanger 8, and then respectively enters the first methanation reactor 1a and the second methanation reactor 1b, and most of H is respectively carried out in the first methanation reactor and the second methanation reactor 2 And CO methanation reaction and byproduct steam, the reaction gas out of the first section of the first low-pressure methanation reactor 1a is subjected to heat exchange and temperature reduction through a first heat exchanger 8, one part of the reaction gas is converged with the purified feed gas entering the first section of the second methanation reactor 1b and then enters the second methanation reactor 1b for reaction, the other part of the reaction gas is subjected to moisture separation through a first water separator 6, then the pressure of the reaction gas is increased to about 10MPa through a compression section of a circulating compressor 2, and then high CH is generated 4 And the circulating gas with low CO content is heated by the second heat exchanger 9 and then mixed with the raw material gas high CO gas entering the first methanation reactor 1a, and the mixture enters the first methanation reactor 1a again for reaction. The reaction gas from the first stage of the second methanation reactor 1b exchanges heat through the second heat exchanger 9, enters the circulating compressor 2, the compressed gas (10MPa) from the compression section of the circulating compressor 2 firstly passes through the second separator 7 to separate moisture, then passes through the third heat exchanger 10 to exchange heat with the reaction gas from the second stage of the methanation reactor 3 and then enters the inlet of the second stage of the methanation reactor 3, the methanation reaction of the rest of carbon oxide and hydrogen is completed, and the reaction gas from the second stage of the methanation reactor is dischargedAnd the reaction gas of the section methanation reactor 3 sequentially passes through a third heat exchanger 10, a water cooler 11 and a third water separator 12, and moisture is separated to obtain SNG.
Example 5
The synthetic ammonia coproduction methanol production device is reformed into a synthetic natural gas peak regulation device:
as shown in figure 8, the original synthetic ammonia production is that the fixed bed coal is gasified by rich oxygen to prepare semi-water gas, and the crude gas is subjected to CO conversion and CO removal 2 Purifying and adjusting H 2 、CO、CO 2 、N 2 Composition H 2 And the composition ratio of CO is adjusted according to the yield ratio of the methanol and the ammonia. The purified synthesis gas is compressed and then enters a methanol synthesis device for synthesizing methanol under 5MPa, the purge gas after synthesizing methanol is compressed and pressurized to 20-25MPa and then enters an ammonia synthesis device for synthesizing ammonia, and the purge gas is transformed into a natural gas peak regulation device for producing a synthetic ammonia plant.
As shown in FIG. 9, H is prepared by changing coal gasification into pure oxygen gasification 2 Introducing CO-rich water gas into CO conversion and purification device to convert H 2 、CO、CO 2 The composition is adjusted to
The pressure of a compressor is increased, a methanol reactor in a low-pressure methanol device is transformed into a heat exchange methanation reactor which strongly transfers heat, and most of CO and H are carried out under the pressure of 4-7 MPa by utilizing equipment such as a heat exchanger, a water cooler, a separator and the like of the methanol device 2 Synthesis of CH 4 . The remaining non-synthesized 10-20% of H in the reaction gas 2 And CO is compressed to high pressure (10-20 MPa) to perform high-pressure methanation synthesis to obtain natural gas, the high-pressure methanation can utilize an ammonia synthesis tower to connect a heat exchange or heat insulation methanation reactor in parallel at an ammonia synthesis inlet and an ammonia synthesis outlet, and simultaneously, the methane synthesis is completed by utilizing equipment such as a heat exchanger, a water cooler and the like of an ammonia synthesis device, and the original ammonia synthesis tower can be transformed into the high-pressure methanation reactor.
Claims (6)
1. A methanation method for preparing synthetic natural gas is characterized in that: the raw material gas purified and deprived of catalyst poison firstly enters a first-stage methanation reactor under the grade of coal gasification and purification pressureMost of H 2 And performing methanation reaction with CO, feeding the reaction gas with CO more than 100ppm into a two-stage methanation reactor to complete methanation reaction of the rest carbon oxide and hydrogen to obtain CH in the methanated dry gas 4 More than 93 percent and the calorific value more than 33MJ/m 3 (ii) a The first-stage methanation reactor is a water-cooling or heat-conducting oil heat-exchange byproduct steam methanation reactor, and the second-stage methanation reactor is a heat-exchange methanation reactor or an adiabatic methanation reactor;
the water-cooling or heat-conducting oil byproduct steam methanation reactor is a wound tube type water-cooling or heat-conducting oil heat exchange byproduct steam methanation reactor; the reaction pressure of the first-stage methanation reactor is 1-6MPa, and the reaction pressure of the second-stage methanation reactor is 1-30MPa higher than that of the first-stage methanation reactor.
2. The methanation process of claim 1, wherein: the raw material gas is coal gasification synthesis gas, the mole percentage of CO in the raw material gas is 10-30%, the raw material gas is subjected to deep purification and heat exchange heating, part of the raw material gas and circulating gas are mixed and enter a first-stage methanation reactor for reaction, the reaction gas which is discharged from the first-stage methanation reactor is mixed with the rest raw material gas and then enters a second-stage methanation reactor, part of the reaction gas which is discharged from the second-stage methanation reactor is subjected to cooling and moisture separation, the pressure of the reaction gas is increased by a circulator, the reaction gas is used as the circulating gas to be converged with part of the synthesis gas which enters the first-stage methanation reactor, and the rest of the reaction gas is used as synthesis natural gas product gas.
3. A methanation method for preparing synthetic natural gas according to claim 1, which comprises a first-stage methanation reactor and a second-stage methanation reactor which are connected in sequence, and is characterized in that: the first-stage methanation reactor is externally connected with steam drum byproduct steam, the first-stage methanation reactor is a water-cooling or heat-conducting oil heat exchange byproduct steam methanation reactor, and the second-stage methanation reactor is a heat exchange methanation reactor or an adiabatic methanation reactor; the water-cooling or heat-conducting oil byproduct steam methanation reactor is a wound tube type water-cooling or heat-conducting oil heat exchange byproduct steam methanation reactor.
4. The apparatus of claim 3, wherein: the device still include first heat exchanger, second heat exchanger, water cooler, circulator and first water separator, one section methanation reactor, two-stage section methanation reactor, first heat exchanger, second heat exchanger, water cooler, first water separator, circulator connect gradually, the export of circulator and second heat exchanger, the import of one section methanation reactor connect gradually.
5. The apparatus of claim 3, wherein: the device still include clarifier, first heat exchanger, second heat exchanger, third heat exchanger, water cooler, recycle compressor, first water separator and second water separator, one section methanation reactor, first heat exchanger, first water separator, recycle compressor connect gradually, the export of clarifier and first heat exchanger, one section methanation reactor's import connect gradually, recycle compressor's compressed gas export and second heat exchanger, two sections methanation reactor connect gradually, two sections methanation reactor's export and second heat exchanger, third heat exchanger, water cooler, second water separator connect gradually, recycle compressor's recycle gas export and one section methanation reactor's access connection, the third heat exchanger be connected with the clarifier.
6. The apparatus of claim 3, wherein: the first-stage methanation reactor comprises two reactors: the device comprises a first methanation reactor, a second methanation reactor, a steam pocket and a water pump, and further comprises a purifier, a first heat exchanger, a second heat exchanger, a third heat exchanger, a water cooler, a first water separator, a second water separator and a circulating compressor, wherein the purifier is connected with the first heat exchanger, the outlet of the first heat exchanger is divided into two paths which are respectively connected with the inlets of the first methanation reactor and the second methanation reactor, the outlet of the first methanation reactor is sequentially connected with the first heat exchanger, the first water separator, the circulating compressor, the second water separator, the third heat exchanger and the second methanation reactor, the outlet of the second methanation reactor is sequentially connected with the third heat exchanger, the water cooler and the second water separator, the circulating gas outlet of the circulating compressor is connected with the inlet of the first methanation reactor, and the outlet of the first-stage second methanation reactor is connected with the second heat exchanger and the circulating compressor in sequence.
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| CN101508922A (en) * | 2009-03-16 | 2009-08-19 | 西南化工研究设计院 | Methanation reaction process using oven gas to prepare substitute natural gas |
| 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 |
| CN103380199A (en) * | 2010-11-11 | 2013-10-30 | 庄信万丰股份有限公司 | Process |
| CN102585950A (en) * | 2012-02-27 | 2012-07-18 | 四川亚连科技有限责任公司 | Method for preparing synthetic natural gas by coke oven gas in combination with straw gas |
| CN102776043A (en) * | 2012-07-30 | 2012-11-14 | 西南化工研究设计院有限公司 | Circulating method for preparing natural gas by multi-stage methanation of semi-coke tail gas |
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