CN104804787A - Methanation method and device for preparation of synthetic natural gas - Google Patents
Methanation method and device for preparation of synthetic natural gas Download PDFInfo
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- CN104804787A CN104804787A CN201410045950.6A CN201410045950A CN104804787A CN 104804787 A CN104804787 A CN 104804787A CN 201410045950 A CN201410045950 A CN 201410045950A CN 104804787 A CN104804787 A CN 104804787A
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Abstract
The invention discloses a methanation method and device for preparation of synthetic natural gas. The method comprises that raw material gas subjected to catalyst poison purification removal enters into a first methanation reactor and undergoes a methanation reaction with most of H2 and CO, and the reaction gas enters into a second methanation reactor and undergoes a methanation reaction with the rest of H2 and CO so that dry gas subjected to methanation has CH4 content greater than 93% and a calorific value greater than 33MJ/M<3>. The invention also discloses a device for implementation of the method. The high-efficiency energy-saving compact large-scale natural gas methanation preparation technology and device are especially suitable for the conditions that many ammonia synthesis factories need coal gasification and purification low pressure apparatuses and ammonia synthesis middle/high pressure apparatuses. Middle and small scale ammonia synthesis factory high-pressure compressor and high-pressure synthesis device in China can be transformed into an artificial natural gas synthesis device so that a large amount of investment is saved. The technology and device have important effects.
Description
Technical field
The present invention relates to technical field of chemical engineering, particularly relate to a kind of methanation process and device of synthetic natural gas processed.
Background technology
External coal process for producing natural, first converts through CO earning again by gasification preparing synthetic gas at present, obtained
synthetic gas, then material synthesis gas methanation is become Sweet natural gas, wherein gordian technique methanation all adopts high-temperature heat insulation methanation, such as the TREMP of Tops φ e company
tMtechnique (Zhu Ruichun etc., " technical study of coal process for producing natural ", " clean coal technology " the 17th volume the 6th phase in 2011, P81-85) Fig. 4, adopt five high-temperature heat insulation reactors in series reactions, other are as also similar in Lurgi and DAVY methanation technology.So technical process is long, equipment is many, investment is large, energy consumption is high.
Current use is containing H
2, CO, CO
2the methanation of methanation Artificial Natural Gas, because of different with unstripped gas, although pressure is also just different, (such as coke oven preparing natural gas is upper and lower at 1MPa, producing synthesis gas from coal methane is as upper and lower in Datang introduction DAVY methane turns to 3MPa), but methanation is substantially all one, front and back pressure ratings, raw gas pressure is lower, and do not pressurize and carry out methanation, low-pressure methane easy control of reaction system, and minimizing power consumption of compressor, but low pressure then equipment is huge, the gas plant of annual output 4000000000 side such as introduced divided for three phases, the first phase is produced more than 13 hundred million sides per year and just establishes A, B bis-covering device, form 4,000,000,000 and can reach 100 multiple stage by power methanation equipment, product Sweet natural gas pipe network is supplied gas, for reducing gas transmission caliber, China's domestic design mostly is 10MPa, also 12MPa is had, product Sweet natural gas after namely for methane need recompress 10MPa, dewater at 40 DEG C also needs through dehydrating with triglycol further again after water is separated, to ensure that gas dew point is at-3 DEG C, make compressed natural gas then pressure more up to 20MPa.Because methanation reaction is contracting volumetric reaction, by following reaction formula:
CO+3H
2=CH
4+H
2O
CO
2+4H
2=CH
4+2H
2O
CH in visible product
4balanced contents
pressure P improves, and greatly improve the balanced contents of methanation in reaction product, high pressure improves again the speed of response of methanation, therefore methanation reaction air speed is improved, air speed V under pressure
p=V
sp
n, in formula, V is air speed under normal pressure, and in formula, the n of pressure P is about 0.4.
Summary of the invention
For overcoming above-mentioned shortcoming of the prior art, this application provides a kind of energy-efficient, compact large-scale preparing natural gas by methanation Technology and device, especially for the situation of numerous synthesis ammonia plant gasification and gas purification to be low-voltage device and synthetic ammonia be mesohigh device, wherein a lot of setting also has mesolow combined production of methanol device, existing equipment can be made full use of and reduce investment, there is very important effect.
For achieving the above object, the present invention takes following technical scheme:
A methanation process for synthetic natural gas processed, the unstripped gas sloughing catalyzer poison through purification first enters one section of methanator and carries out most of H under gasification and purification pressure rating
2with CO methanation reaction, the methanation reaction that two sections of methanators complete all the other carbonoxides and hydrogen is entered to the reaction gas of CO>0.5% again, to reach after methanation CH in dry gas
4>93%, calorific value >33MJ/M
3; One section of described methanator is water-cooled or thermal oil heat exchange byproduct steam methanator, and two sections of described methanators are heat exchange methanator or adiabatic methanation reactor
Described water-cooled or thermal oil byproduct steam methanator are around pipe-type water-cooling or thermal oil heat exchange byproduct steam methanator.
Described unstripped gas is synthesis gas from coal gasification, in described unstripped gas, CO molar percentage is 10 ~ 30%, described unstripped gas is through deep purifying, heat exchange heats up, partial raw gas and circulation gas are mixed into one section of methanator and react, the reaction gas going out one section of methanator mixes laggard two sections of methanators with all the other unstripped gass, the reaction gas going out two sections of methanators boosts through circulator through a refrigerated separation moisture time part, the synthetic gas entering one section of methanator as circulation gas and part converges, rest part is as synthetic natural gas gas product.
One section of described methanator reaction pressure is 2-6MPa.
Two sections of described methanator reaction pressures improve 1-30MPa than one section of methanation reaction.
A kind of methanation device for synthetic natural gas processed as above, comprise the one section of methanator and two sections of methanators that connect successively, the described external drum byproduct steam of one section of methanator, one section of described methanator is water-cooled or thermal oil heat exchange byproduct steam methanator, and two sections of described methanators are heat exchange methanator or adiabatic methanation reactor.
Described water-cooled or thermal oil byproduct steam methanator are thermal oil heat exchange byproduct steam methanators after pipe-type water-cooling.
Described device also comprises First Heat Exchanger, the second interchanger, water cooler, circulator and the first water separator, one section of described methanator, two sections of methanators, First Heat Exchanger, the second interchanger, water cooler, the first water separator, circulators connect successively, and the outlet of described circulator is connected successively with the import of the second interchanger, one section of methanator.
Described device also comprises cleaner, First Heat Exchanger, second interchanger, 3rd interchanger, water cooler, recycle compressor, first water separator and the second water separator, one section of described methanator, First Heat Exchanger, first water separator, recycle compressor connects successively, the outlet of described cleaner and First Heat Exchanger, the import of one section of methanator connects successively, compressed gas outlet and second interchanger of described recycle compressor, two sections of methanators connect successively, the outlet of two sections of described methanators and the second interchanger, 3rd interchanger, water cooler, second water separator connects successively, the circulation gas outlet of described recycle compressor is connected with the import of one section of methanator, the 3rd described interchanger is connected with cleaner.
One section of described methanator has two: one section of first methanator and one section of second methanator, each external drum and water pump, and described device also comprises cleaner, First Heat Exchanger, second interchanger, 3rd interchanger, water cooler, first water separator, second water separator and recycle compressor, described cleaner is connected with First Heat Exchanger, and described First Heat Exchanger outlet is divided into two tunnels, is connected respectively with the import of one section of first methanator and one section of second methanator, , one section of first described methanator outlet and First Heat Exchanger, first water separator, recycle compressor, second water separator, 3rd interchanger, two sections of methanators connect successively, the outlet of two sections of described methanators and the 3rd interchanger, water cooler, second water separator connects successively, the import of circulation gas outlet connection one section of first methanator of described recycle compressor, one section of second described methanator outlet and the second interchanger, recycle compressor connects successively.
The present invention has following beneficial effect:
1. change built, external introduction DAVY, Lurgi, Tops φ e high-temperature heat insulation preparing natural gas by methanation technology of building at present, by methanation reaction, heat exchange, byproduct steam triplicity, significantly simplify flow process, minimizing equipment, investment reduction, improves efficiency, reduce costs, increase the benefit.
2. efficient, later stage high pressure is conducive to improving final synthetic ratio, reduces catalytic amount.
3. energy-conservation, high pressure improves separation byproduct water effect, meets the high pressure requirement of compressed natural gas processed or pipe network conveying.
4. be conducive to larger-scale unit, improve single wire device synthetic natural gas ability.
5. middle-size and small-size ammonia factory of China high pressure compressor can be utilized with high-pressure synthesizer scrap build to become synthesis Artificial Natural Gas device, save great amount of investment.
Accompanying drawing explanation
Fig. 1 is the principle process schematic block diagram of the inventive method.
Fig. 2 is the schematic block diagram of a kind of embodiment of the inventive method.
Fig. 3 is the schematic block diagram of the another kind of embodiment of the inventive method, comprising a heat exchange and secondary heat exchange.
Fig. 4 is the schematic diagram of a kind of embodiment of apparatus of the present invention.
Fig. 5 is the schematic diagram of the another kind of embodiment of apparatus of the present invention, and wherein interchanger has two.
Fig. 6 is the schematic diagram of the another kind of embodiment of apparatus of the present invention, and wherein interchanger has three, and water separator has two.
Fig. 7 is the schematic diagram of the another kind of embodiment of apparatus of the present invention, and wherein one section of methanator has two.
Fig. 8 is the former synthetic ammonia coproducing methanol Production Flow Chart schematic diagram in the embodiment of the present invention 5.
Fig. 9 is the improved synthetic natural gas peak regulation schematic flow sheet in the embodiment of the present invention 5.
Description of reference numerals:
1-mono-section of methanator 2-recycle compressor 3-bis-sections of methanators
4-drum 5-cleaner 6-first water separator
7-second water separator 8-First Heat Exchanger 9-second interchanger
10-the 3rd interchanger 11-water cooler 12-the 3rd water separator
1a-mono-section of first methanator 1b-mono-section of second methanator 13-circulator
14-vapour generator
Embodiment
Describe the present invention below in conjunction with drawings and Examples.
Embodiment 1
The methanation basic device for synthetic natural gas processed as shown in Figure 4, comprise the one section of methanator 1, recycle compressor 2, two sections of methanators 3, water cooler 11 and the first water separator 6 that connect successively, one section of described methanator 1 external drum 4 byproduct steam, described one section of methanator 1 is around pipe heat exchange type reactor, and described two sections of methanators 3 are adiabatic reactor.
In the present embodiment, one section of methanation synthesis pressure 3 ~ 6MPa, two sections of methanation synthesis pressure 10MPa, the pressure of two sections of methanators 3 is higher than one section of methanator 1.
When said apparatus runs, the unstripped gas after purification first carries out most of H in gasification and purification pressure rating (such as 3 ~ 6MPa) inferior being pressed in one section of methanator 1 of byproduct steam
2with CO methanation reaction, temperature of reaction 250 ~ 500 DEG C, then reaction gas enters recycle compressor 2 and circulates, pressurizes, partial reaction gas goes to reduce CO content gas with the gas and vapor permeation entering one section of methanator 1 from circulation section outlet, remaining gas removes the methanation reaction completing all the other carbonoxides and hydrogen in two sections of methanators 3 after compression after 10MPa, to reach after methanation CH in dry gas
4>93%, calorific value >33MJ/M
3, final reaction gas obtains SNG through water cooler 11, first water separator 6 successively.
Embodiment 2
The methanation device for synthetic natural gas processed as shown in Figure 5, comprise one section of methanator, 1, two sections of methanators 3, First Heat Exchanger 8, second interchanger 9, water cooler 11, circulator 13 and the first water separator 6, one section of described methanator, 1, two sections of methanators 3, First Heat Exchanger 8, second interchanger 9, water cooler 11, first water separator 6, circulator 13 connect successively, and the import of outlet and the second interchanger 9, one section of methanator 1 of described circulator 13 is connected successively.
When said apparatus runs, unstripped gas after purification is warmed up to 250 ~ 300 DEG C through First Heat Exchanger 8 and reaction gas heat exchange, unstripped gas is divided into two strands afterwards, one unstripped gas enters one section of methanator 1, react at about 400 DEG C, the reaction gas going out one section of methanator 1 enters two sections of methanators 3, go out the reaction gas of two sections of methanators 3 successively through First Heat Exchanger 8, second interchanger 9, water cooler 11 cools to 40 DEG C, after the most laggard first water separator 6 is separated moisture content, a part is as sintetics gas, another part enters circulator 13 and goes and the unstripped gas mixing synthesizing methane entering one section of methanator 1 as circulation gas.Embodiment 3
Device as shown in Figure 6, described device comprises cleaner 5, one section of methanator 1, two sections of methanators 3, First Heat Exchanger 8, second interchanger 9, 3rd interchanger 10, water cooler 11, first water separator 6, second water separator 7, vapour generator 14, one section of described methanator 1, First Heat Exchanger 8, first water separator 6, the recycle compressor 2 be made up of circulation section and compression section, second interchanger 9, two sections of methanators 3, the outlet of two sections of described methanators 3 again with the second interchanger 9, 3rd interchanger 10, water cooler 11, second water separator 7 connects successively, the compression section export pipeline of wherein said recycle compressor 2 is connected with the second interchanger 9, be connected with high-pressure methanation reactor 3 import again, the export pipeline of described earning device 5 first through First Heat Exchanger 8, then converge with recycle compressor 2 circulation section export pipeline after be connected the import of one section of methanator 1.One section of described methanator 1 steam-out (SO) producer 14, uses thermal oil heat exchange byproduct steam in described vapour generator 14.
When said apparatus runs, pressure is that the unstripped gas of 3 ~ 6MPa is first heated laggard cleaner 5 deep purifying about 210 DEG C through the 3rd interchanger 10 by reaction gas, then unstripped gas is warmed up to after about 250 DEG C through First Heat Exchanger 8 and the reaction gas heat exchange going out one section of methanator 1, converge with circulation gas and enter one section of methanator 1, carry out most of H
2with CO methanation reaction, reaction heat is managed interior thermal oil gasification heat absorption and is taken out of, and one section of methanator 1 steam-out (SO) producer 14, adopts thermal oil heat exchange in the pipe of vapour generator 14, byproduct steam.The reaction gas (temperature about 300 ~ 500 DEG C) going out one section of methanator 1 separates part moisture content through laggard first water separator 6 (about 40 DEG C) of First Heat Exchanger 8 heat exchange cooling, residue reaction gas enters recycle compressor 2, portion gas mixes from circulation section outlet with the unstripped gas entering one section of methanator 1 afterwards, remaining gas is compressed to 12MPa through the outlet of the compression section of recycle compressor 2 and enters the second interchanger 9, compressed gas enters the methanation reaction that two sections of methanators 3 complete all the other carbonoxides and hydrogen again after the second interchanger 9 heats up (about 250 DEG C), go out the reaction gas of two sections of methanators 3 successively through the second interchanger 9, 3rd interchanger 10, water cooler 11 and the second water separator 7, obtain SNG.Said apparatus is applicable to unstripped gas for being the richest in alkanisation gas (CH
4>10%) reaction conditions.
Embodiment 4
Device as shown in Figure 7, when unstripped gas coal water slurry or coal gasification, CH in composition
4low and the H of content
2, CO content very high time, react too violent at the beginning for avoiding methanation, one section of described methanator adopts two: an one section of first methanator 1a and section the second methanator 1b, each external drum and pump, described device also comprises cleaner 5, First Heat Exchanger 8, second interchanger 9, the 3rd interchanger 10, water cooler 11, first water separator 6, second water separator 7 and the 3rd water separator 12 except recycle compressor 2, two sections of methanators 3.The export pipeline of described cleaner 5 is divided into two tunnels after by First Heat Exchanger 8, be connected with one section of first methanator 1a and a section of the second methanator 1b respectively, namely one section of first methanator 1a and a section of the second methanator 1b is in parallel, the outlet of one section of first methanator 1a is divided into two tunnels after First Heat Exchanger 8, one tunnel is connected with the pipeline entering one section of second methanator 1b, another road connects the first water separator 6 and recycle compressor 2 successively, the outlet of one section of second methanator 1b is connected with the compression section import of recycle compressor 2 after the second interchanger 9.The outlet of described recycle compressor 2 is divided into circulation section to export and compression section outlet, and described circulation section outlet is connected with the import of one section of first methanator 1a after the second interchanger 9, and described compression section outlet is connected with the second water separator 7.The outlet of the second described water separator 7 is connected successively with two sections of methanators 3, the 3rd interchanger 10, water cooler 11, the 3rd water separator 12 after the 3rd interchanger 10.
When said apparatus runs, unstripped gas advanced cleaner 5 deep purifying removing catalyzer poison, then after First Heat Exchanger 8 is heated up by the reaction gas heat exchange going out one section of first methanator 1a, enter one section of first methanator 1a and a section of the second methanator 1b respectively, in two reactors, carry out most of H respectively
2with CO methanation reaction and byproduct steam, go out the reaction gas of one section of first low-pressure methane reactor 1a after First Heat Exchanger 8 heat exchange cooling, after a part and the purification of entering one section of second methanator 1b, unstripped gas converges laggard second methanator 1b and reacts, and another part is separated after moisture content laggard recycle compressor 2 compression section boosts to about 10MPa through the first water separator 6 and has generated high CH
4, low CO content circulation gas, circulation gas after the second interchanger 9 heats with enter the unstripped gas height CO gas and vapor permeation of one section of first methanator 1a, enter one section of first methanator 1a again and react.Go out the reaction gas of one section of second methanator 1b through the second interchanger 9 heat exchange, enter recycle compressor 2, first moisture content is separated through the second separator 7 from compression section compressed gas out (10MPa) of recycle compressor 2, the import of two sections of methanators 3 is entered again after the 3rd interchanger 10 with the reaction gas heat exchange going out two sections of methanators 3, complete the methanation reaction of all the other carbonoxides and hydrogen, go out the reaction gas of two sections of methanators 3 successively through the 3rd interchanger 10, water cooler 11 and the 3rd water separator 12, be separated moisture content and obtain SNG.
Embodiment 5
Synthetic ammonia coproducing methanol production equipment is transformed into synthetic natural gas peak adjusting device:
As shown in Figure 8, original Ammonia Production is fixed bed coal oxygen-rich gasification semi-water gas, and raw gas is through CO conversion and take off CO
2h is adjusted in purification
2, CO, CO
2, N
2composition, H
2, CO proportion of composing is according to methyl alcohol and hydrazine yield proportion adjustment.5MPa synthesizing methanol in the compressed laggard synthesizing methanol device of decontaminating syngas, after synthesizing methanol, the compressed 20-25MPa of being pressurized to of periodic off-gases enters ammonia synthesizer synthetic ammonia, and the existing synthesis ammonia plant that is transformed into produces natural gas peak-shaving device.
As shown in Figure 9, change gasification into pure oxygen gasification and obtain H
2, CO high-content water-gas, enter CO conversion, refining plant is by H
2, CO, CO
2composition is adjusted to
through compressor boosting, the methanol reactor in low-pressure methanol unit is transform as the heat exchange methanator of the present invention moving by force heat, and utilize the equipment such as interchanger, water cooler, separator of methanol device, under 4 ~ 7MPa pressure, carry out most of CO, H
2synthesis CH
4.About 10% ~ the 20%H do not synthesized is remained in reaction gas
2, CO is compressed to high pressure (10 ~ 20MPa) and carries out high pressure methane and be combined to obtained Sweet natural gas, high-pressure methanation can utilize ammonia synthesis converter to import and export a heat exchange in parallel or adiabatic methanation reactor in ammonia synthesis, utilize the equipment such as the interchanger of ammonia synthesizer, water cooler to complete methane synthesis simultaneously, also can transform high-pressure methanation reactor as with former ammonia synthesis converter.
Claims (10)
1. a methanation process for synthetic natural gas processed, is characterized in that: the unstripped gas sloughing catalyzer poison through purification first enters one section of methanator and carries out most of H under gasification and purification pressure rating
2with CO methanation reaction, the methanation reaction that two sections of methanators complete all the other carbonoxides and hydrogen is entered to the reaction gas of CO>100ppm again, to reach after methanation CH in dry gas
4>93%, calorific value >33MJ/M
3; One section of described methanator is water-cooled or thermal oil heat exchange byproduct steam methanator, and two sections of described methanators are heat exchange methanator or adiabatic methanation reactor.
2. the methanation process of synthetic natural gas processed according to claim 1, is characterized in that: described water-cooled or thermal oil byproduct steam methanator are around pipe-type water-cooling or thermal oil heat exchange byproduct steam methanator.
3. the methanation process of synthetic natural gas processed according to claim 1, it is characterized in that: described unstripped gas is synthesis gas from coal gasification, in described unstripped gas, CO molar percentage is 10 ~ 30%, described unstripped gas is through deep purifying, heat exchange heats up, partial raw gas and circulation gas are mixed into one section of methanator and react, the reaction gas going out one section of methanator mixes laggard two sections of methanators with all the other unstripped gass, the reaction gas going out two sections of methanators boosts through circulator through refrigerated separation moisture content rear portion, the synthetic gas entering one section of methanator as circulation gas and part converges, rest part is as synthetic natural gas gas product.
4. the methanation process of synthetic natural gas processed according to claim 1, is characterized in that: one section of described methanator reaction pressure is 1-6MPa.
5. the methanation process of synthetic natural gas processed according to claim 1, is characterized in that: two sections of described methanator reaction pressures improve 1-30MPa than one section of methanation reaction.
6. the methanation device for synthetic natural gas processed as claimed in claim 1, comprise the one section of methanator and two sections of methanators that connect successively, it is characterized in that: the described external drum byproduct steam of one section of methanator, one section of described methanator is water-cooled or thermal oil heat exchange byproduct steam methanator, and two sections of described methanators are heat exchange methanator or adiabatic methanation reactor.
7. the methanation device of synthetic natural gas processed as claimed in claim 6, is characterized in that: described water-cooled or thermal oil byproduct steam methanator are around pipe-type water-cooling or thermal oil heat exchange byproduct steam methanator.
8. the methanation device of synthetic natural gas processed as claimed in claim 6, it is characterized in that: described device also comprises First Heat Exchanger, the second interchanger, water cooler, circulator and the first water separator, one section of described methanator, two sections of methanators, First Heat Exchanger, the second interchanger, water cooler, the first water separator, circulators connect successively, and the outlet of described circulator is connected successively with the import of the second interchanger, one section of methanator.
9. the methanation device of synthetic natural gas processed as claimed in claim 6, it is characterized in that: described device also comprises cleaner, First Heat Exchanger, second interchanger, 3rd interchanger, water cooler, recycle compressor, first water separator and the second water separator, one section of described methanator, First Heat Exchanger, first water separator, recycle compressor connects successively, the outlet of described cleaner and First Heat Exchanger, the import of one section of methanator connects successively, compressed gas outlet and second interchanger of described recycle compressor, two sections of methanators connect successively, the outlet of two sections of described methanators and the second interchanger, 3rd interchanger, water cooler, second water separator connects successively, the circulation gas outlet of described recycle compressor is connected with the import of one section of methanator, the 3rd described interchanger is connected with cleaner.
10. the methanation device of synthetic natural gas processed as claimed in claim 6, it is characterized in that: one section of described methanator has two: one section of first methanator and one section of second methanator, each external drum and water pump, described device also comprises cleaner, First Heat Exchanger, second interchanger, 3rd interchanger, water cooler, first water separator, second water separator and recycle compressor, described cleaner is connected with First Heat Exchanger, and described First Heat Exchanger outlet is divided into two tunnels, is connected respectively with the import of one section of first methanator and one section of second methanator, , one section of first described methanator outlet and First Heat Exchanger, first water separator, recycle compressor, second water separator, 3rd interchanger, two sections of methanators connect successively, the outlet of two sections of described methanators and the 3rd interchanger, water cooler, second water separator connects successively, the import of circulation gas outlet connection one section of first methanator of described recycle compressor, one section of second described methanator outlet and the second interchanger, recycle compressor connects successively.
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| CN106994320A (en) * | 2017-04-11 | 2017-08-01 | 淄博赢信达知识产权咨询服务有限公司 | The vertical axial stream that oil plant low pressure gasifying moves heat easily adjusts self limiting temperature reactor |
| CN109701454A (en) * | 2019-01-28 | 2019-05-03 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation, which goes into operation, recycles heat riser |
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Cited By (5)
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| CN105645581A (en) * | 2016-03-22 | 2016-06-08 | 北京化工大学 | System device and method for synchronously realizing organic waste disposal and synthesis gas quality improvement |
| CN105645581B (en) * | 2016-03-22 | 2018-04-03 | 北京化工大学 | It is a kind of synchronously to realize organic waste treatment and the system and device and method of synthesis gas upgrading |
| CN106994320A (en) * | 2017-04-11 | 2017-08-01 | 淄博赢信达知识产权咨询服务有限公司 | The vertical axial stream that oil plant low pressure gasifying moves heat easily adjusts self limiting temperature reactor |
| CN109701454A (en) * | 2019-01-28 | 2019-05-03 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation, which goes into operation, recycles heat riser |
| CN109701454B (en) * | 2019-01-28 | 2024-02-13 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation start-up circulation heating device |
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| CN104804787B (en) | 2022-09-13 |
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