CN101723324A - Method for preparing synthetic gas by utilizing thermal coupling fixed bed device - Google Patents
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- CN101723324A CN101723324A CN200910259881A CN200910259881A CN101723324A CN 101723324 A CN101723324 A CN 101723324A CN 200910259881 A CN200910259881 A CN 200910259881A CN 200910259881 A CN200910259881 A CN 200910259881A CN 101723324 A CN101723324 A CN 101723324A
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Abstract
The invention relates to a method for preparing synthetic gas by utilizing a thermal coupling fixed bed device, which comprises the following process steps of: preheating natural gas and oxygen through a reactor heat exchange region, then spraying into an oxidation region through a nozzle for complete oxidation and partial oxidation reactions, increasing the generation proportion of the synthetic gas under the actions of a guide ceramic and a high temperature catalysis resistant partial oxidation catalyst, flowing into a reforming region after the material temperature decreases to the permissible reaction temperature of a reforming catalyst, generating a reforming reaction under the action of the reforming catalyst, and finally discharging the synthetic gas as a product after the rapid heat exchange of the heat exchange region. The new method for preparing the synthetic gas not only reserves the advantages of high efficiency and high selectivity of preparing the synthetic gas through laboratory scale natural gas catalytic partial oxidation, but also decreases the hot-spot temperature of a bed layer, relieves the generation of deposited carbon, can fully utilize the heat released by an oxidation reaction, enables the target response temperature to reach more than 1000 DEG C, greatly improves the utilization efficiency of substances and energy and has important industrial application prospects.
Description
Technical field
The invention provides a kind of method of utilizing the Sweet natural gas preparing synthetic gas, especially utilize a kind of thermal coupling fixed bed device to prepare the method for synthetic gas, particularly is to belong to Sweet natural gas catalyzing part oxidation preparing synthetic gas self-heating conversion method.
Background technology
At present, 90% gas chemical industry utilization realizes by the Sweet natural gas synthetic gas production process in the world.Therefore, gas chemical industry's key problem in technology is the preparation of synthetic gas.From catalysis technique, reaction process and engineering many-side different combinations is carried out in the principal reaction (comprising steam reformation, CO 2 reformation, catalysis and non-catalytic complete oxidation and partial oxidation) of Sweet natural gas preparing synthetic gas, coupling and comprehensive utilization by energy, developed and the diversified forms of association reforming process, its core objective is realized the utilization of Sweet natural gas synthetic gas production process energy optimization exactly, thus the productive expense of the process of reduction.Representative technology has: the self-heating recapitalization technology (ATR) of the associating self-heating recapitalization technology (CAR) of heat exchange/reforming process of Kellogg (KRES), Uhde, the gas heating reforming process (GHR) of ICI, Topsoe, the catalyzing part oxidation (CPO) of ExxonMobil etc.
The something in common of above-mentioned various associating reforming process technology is, traditional steam reformation or steam reformation-self-heating recapitalization two-section joint reforming process are reformed and reformed, make the oxidizing reaction of the reforming reaction of heat absorption and heat release logistics, can be able to sufficient coupling by stream, thereby the material consumption and the energy consumption of the process of reduction.The development of these processes shows, the Sweet natural gas synthetic gas production process just gradually from water be the steam reformation of one of main raw material progressively to being that the burning-reformation of one of main raw material and partial oxidation change with oxygen, its core technology feature is with the CPO process of gentle heat release and the steam reformation PROCESS COUPLING of strong heat absorption.Therefore, the successful exploitation of coupling process in fact also just becomes the key of high-efficiency and energy-saving type synthesis gas preparation process development.
In order to adapt to the higher working pressure in most of downstreams and to consider from the economy of whole process, synthetic gas production process need high pressure (＞carry out under 2MPa).Yet under high pressure, be subjected to the restriction of thermodynamic(al)equilibrium, expect comparatively ideal methane conversion and synthetic gas selectivity, goal response (reforming reaction) temperature must be above 1000 ℃.At present traditional reforming process temperature of reaction is lower, generally about 900 ℃, can not satisfy the demands.Obviously, obtain higher synthetic gas yield down, must solve following problems on the engineering in order to realize high temperature, high pressure:
(1) mixed problem of pyroreaction raw material.Consider the difficulty of the outside heat supply of process, have only by improving the material inlet temperature to guarantee that follow-up reforming reaction temperature reaches more than 1000 ℃ that calculation of thermodynamics shows that the preheating temperature of reaction raw materials need reach more than 600 ℃.Under so high preheating temperature, if Sweet natural gas enters reactor after being pre-mixed with oxygen again, because there is limits of explosion in mixture, the security of will certainly influence process operating.Therefore, raw material just can enter reactor after the preheating respectively and carries out contact reacts.
(2) coupling of thermopositive reaction and thermo-negative reaction fast.If raw material enters remix behind the reactor, then in the reactor content ingress, complete oxidation will take place earlier with Sweet natural gas in oxygen, generate carbonic acid gas and water, and emit a large amount of heats, the reforming reaction of heat absorption takes place in unreacted Sweet natural gas again with carbonic acid gas and water, generate synthetic gas.Because the speed of reaction of methane complete oxidation is higher than the speed of reforming reaction far away, therefore, two districts will inevitably occur in reactor: i.e. the strong heat absorption reforming reaction district at reactor forward strong exothermal reaction district and reactor rear portion.In heat release zone, can not in time shift as a large amount of reaction heat, high temperature hotspot will appear, cause unreacted methane generation cracking, cause the serious carbon distribution of catalyzer; In strong heat absorption district, if the required heat of postreaction in time, temperature of reaction will reduce fast, be difficult to obtain ideal methane conversion and synthetic gas selectivity.
As can be seen from the above analysis, be to obtain ideal methane conversion and synthetic gas selectivity, the partial oxidation reaction of the gentle heat release of generation that oxidation zone will be as much as possible, and make temperature of charge drop to the temperature of reaction that follow-up reforming catalyst is allowed; Reformer section should maintain under the high as far as possible temperature reacts.How to regulate and control this two reaction zones, just become formation that suppresses high temperature hotspot and the key that improves the synthetic gas productive rate.
Summary of the invention
The invention provides a kind of method of utilizing the thermal coupling fixed bed device preparing synthetic gas, this method effectively the be coupled oxidizing reaction of strong heat release and the reforming reaction of strong heat absorption, simultaneously, unstripped gas preheating and synthetic gas cooling two portions have been coupled, greatly reduce the bed hot(test)-spot temperature, alleviated the generation of carbon distribution, and can make full use of the oxidizing reaction liberated heat, the reforming reaction temperature is reached more than 1000 ℃, improved the matter and energy utilization ratio.
The object of the present invention is to provide a kind of method that is used for the Sweet natural gas preparing synthetic gas, by means of thermal coupling fixed bed device, make Sweet natural gas and oxygen after the heat transfer zone preheating, be injected to oxidation zone generation oxidizing reaction by nozzle, under the effect of water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst, increase the generation ratio of synthetic gas, temperature of charge flow into reformer section after being reduced to the temperature of reaction that reforming catalyst allows, reforming reaction takes place under the effect of reforming catalyst, at last, the product synthetic gas is discharged after the quick heat exchange of heat transfer zone.The heat that has guaranteed between oxidizing reaction and the reforming reaction that is provided with of water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst is coupled, heat transfer zone the fast cooling that has guaranteed synthetic gas is set, avoided synthetic gas to generate the generation of the reversed reaction of methane after leaving beds, the application of nozzle has guaranteed the mixed effect of unstripped gas.
Purpose of the present invention can be achieved through the following technical solutions.
The invention provides a kind of method of utilizing the thermal coupling fixed bed device preparing synthetic gas, it is characterized in that: this method is implemented in following fixed bed device, it comprises heat transfer zone, oxidation zone, reformer section, thermal insulation layer, nozzle and high pressure resistant metal shell, described oxidation zone and reformer section have adopted the concentric type structure, oxidation zone epimere filling water conservancy diversion pottery, hypomere loads high temperature resistant catalytic partial oxidation catalyst, reformer section is loaded high temperature resistant reforming catalyst, thermal insulation layer is positioned at outside the outer tube, and thermal insulation layer is outward high pressure resistant metal shell; Described heat transfer zone is positioned at the top of device, and unstripped gas and synthetic gas carry out heat exchange at this; Described nozzle is outer mix type nozzle, is installed in the top of oxidation zone; The described method for preparing synthetic gas comprises: Sweet natural gas and oxygen at first enter heat transfer zone and carry out preheating, be injected to oxidation zone through nozzle then and carry out complete oxidation and partial oxidation reaction, under the effect of water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst, increase the generation ratio of synthetic gas, material (unreacting material and resultant) temperature flow into reformer section after being reduced to the temperature of reaction that reforming catalyst allows, reforming reaction takes place under the effect of reforming catalyst, at last, product synthetic gas (main component CO and H
2) after the quick heat exchange of heat transfer zone, discharge.
Consider the difficulty of the outside heat supply of process, have only by improving the raw material gas inlet temperature, guarantee that follow-up reforming reaction temperature reaches more than 1000 ℃, calculation of thermodynamics shows, the preheating temperature of reaction raw materials need reach more than 600 ℃, and the present invention reaches the purpose that is preheating to this temperature by heat transfer zone is set.Enter about 1000 ℃ of the synthetic gas temperature of heat transfer zone, can make unstripped gas be preheating to target temperature by suitable heat interchanging area.
The heat transfer zone of above-mentioned thermal coupling fixed bed device, Sweet natural gas inlet pipe and oxygen intake pipe all are to adopt the serpentine tube structure, and become the adverse current indirect thermal to change with synthesis gas flow, purpose is to increase heat interchanging area, is beneficial to the preheating of unstripped gas and the fast cooling of synthetic gas.If in time do not reduce the synthetic gas temperature, at high temperature, synthetic gas may generate the reversed reaction of methane, reduces the synthetic gas yield; If unstripped gas is not preheating to suitable temperature, follow-up reforming reaction temperature does not just reach expection and sets the goal.
Method of the present invention preferably is 0.45-0.65 at oxygen/Sweet natural gas ratio, and pressure is 0.1-5MPa, and Sweet natural gas ejection speed is greater than the oxygen spouting velocity, and the reforming reaction temperature is 1000-1100 ℃, and the Sweet natural gas air speed is 1000-1.5 * 10
5h
-1Condition under carry out.
The synthetic gas H that the present invention makes
2/ CO ratio is 2: 1, is suitable for reaction process such as downstream methyl alcohol, F-T is synthetic.
In order to reach uniform purpose of Sweet natural gas and oxygen mix and effect, fixed bed device used in the present invention adopts the feeding manner by nozzle material-feeding, and nozzle is positioned at the oxidation zone top; This method comprises: complete oxidation and partial oxidation reaction after nozzle is injected to oxidation zone by duct separately, take place through the heat transfer zone preheating in Sweet natural gas and oxygen at once after the ejection.If mix inhomogeneously, will produce methane rich district and oxygen-rich area, at oxygen-rich area, methane generation complete oxidation emit a large amount of heat, and this part heat is not removed fully, will produce high temperature hotspot; In the methane rich district,, shorten the running period of reaction if the methane overstand under so high temperature, will cracking take place and produces carbon distribution.
In order to reach the reasonable utilization of energy, fixed bed device used in the present invention mainly adopts the concentric type structure, the reforming reaction of the oxidizing reaction of the strong heat release that has been coupled and strong heat absorption; This method comprises: unstripped gas is injected to oxidation zone by nozzle after the heat transfer zone heating, and generation complete oxidation and partial oxidation reaction, emit a large amount of heats, the outer reformer section of pipe in part heat is delivered to by tube wall, and most of heat makes material reach very high temperature, but under the effect of water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst, generate the increase of ratio along with synthetic gas, temperature of charge will decrease, flow into reformer section after reaching the temperature of reaction that reforming catalyst allows, reforming reaction takes place under the effect of reforming catalyst generate synthetic gas, further improved the synthetic gas yield, at last, synthetic gas is discharged by the synthetic gas air outlet after heat transfer zone is cooled off fast.
For the better above said energy coupling of explanation, carried out following design calculation, assumed condition is as follows: the unstripped gas charge ratio is O
2/ CH
4=0.5, preheating temperature is 600 ℃, and oxygen is at oxidation zone complete reaction, CH
4Complete oxidation generates CO
2And H
2O, CH
4Partial oxidation reaction generates CO and H
2, CH
4The per-cent that partial oxidation takes place is the generation ratio of synthetic gas.Thermosteresis is designated as 15%, and 10% reaction heat wherein is to be delivered to the outer wall reformer section by partition.CH
4Temperature of charge under the partial oxidation different ratios is as shown in the table.
| ?CH 4Partial oxidation per-cent (%) | ?CH 4Complete oxidation per-cent (%) | Unreacted CH 4Per-cent (%) | Material | Temperature (℃) |
| ?50 | ?12.5 | ?37.5 | CH 4，CO 2，H 2O，H 2，CO | ?1536 |
| ?60 | ?10 | ?30 | CH 4，CO 2，H 2O，H 2，CO | ?1391 |
| ?70 | ?7.5 | ?22.5 | CH 4，CO 2，H 2O，H 2，CO | ?1284 |
| ?80 | ?5 | ?15 | CH 4，CO 2，H 2O，H 2，CO | ?1128 |
| ?90 | ?2.5 | ?7.5 | CH 4，CO 2，H 2O，H 2，CO | ?972 |
From table as can be seen, when synthetic gas generates ratio when 50% increases to 90%, temperature of charge will drop to 972 ℃ from 1536 ℃, and therefore when synthetic gas generation ratio acquired a certain degree, temperature of charge just can drop to the temperature of reaction that reforming catalyst is allowed.Realize that oxidation zone and reformer section heat coupled key are exactly to control the generation ratio of synthetic gas, so the reactor used Fig. 1 of the present invention is provided with water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst in oxidation zone, be exactly to generate ratio in order to improve synthetic gas in oxidation zone.The water conservancy diversion pottery can make mixing of materials more even, and high temperature resistant catalytic partial oxidation catalyst can be accelerated the speed of reaction of gas by partial oxidation of natural.
In addition, calculating shows, the synthetic gas production rate reaches near 90% the time, temperature has just dropped to 1000 ℃, reactor shown in Figure 1 just in time can carry out replenishing of energy to this part by the heat of partition transmission, temperature of reaction is brought up to more than 1000 ℃, further improved methane conversion and synthetic gas yield.The temperature of reactor distribution situation is seen Fig. 3.Reactor heat coupling principle shown in Figure 2 is similar to above explanation, and this paper is not repeated.The temperature of reactor distribution situation is seen Fig. 4.
The method of preparing synthetic gas of the present invention comprises the reaction of being undertaken by catalyzer, therefore in above-mentioned reactor charge catalyzer is arranged, this catalyzer can be any catalyzer that is applicable to catalyzing part oxidation, steam reforming and CO 2 reformation, but employed catalyzer should satisfy the active and stable not breakable requirement of selectivity in the cycle of long-term operation continuously.Optimum method is an oxidation zone epimere filling water conservancy diversion pottery, and hypomere loads high temperature resistant catalytic partial oxidation catalyst, and reformer section is partly loaded high temperature resistant reforming catalyst, can load water conservancy diversion pottery or inert material at reactor bottom and reformer section catalyzer top.High temperature resistant catalytic partial oxidation catalyst loadings should be able to guarantee that temperature of charge is reduced to the desired temperature of reaction of reforming catalyst.
In the whole process of preparation synthetic gas of the present invention, the reaction bed temperature of reactor is basicly stable more than 1000 ℃, high temperature hotspot and low temperature spot can not appear, guaranteed that the successful reaction self-heating carries out, improved the yield of methane conversion and synthetic gas, substantially near the thermodynamic(al)equilibrium level.
Description of drawings
Fig. 1: Sweet natural gas preparing synthetic gas thermal coupling reaction unit 1 structural representation;
Fig. 2: Sweet natural gas preparing synthetic gas thermal coupling reaction unit 2 structural representations;
Fig. 3: Sweet natural gas preparing synthetic gas thermal coupling reaction unit 1 temperature distribution synoptic diagram;
Fig. 4: Sweet natural gas preparing synthetic gas thermal coupling reaction unit 2 temperature distribution synoptic diagram.
Drawing reference numeral:
1-Sweet natural gas inlet mouth 2-serpentine tube 3-nozzle
The high temperature resistant reforming catalyst of 4-oxidation zone 5-
The high temperature resistant catalytic partial oxidation catalyst of 6-
7-outer tube 8-synthetic gas air outlet 9-oxygen inlet mouth
Pipe in the 10-heat transfer zone 11-water conservancy diversion pottery 12-
The high pressure resistant metal shell of 13-reformer section 14-thermal insulation layer 15-
17-Sweet natural gas air outlet, 16-oxygen air outlet
Embodiment
Describe the present invention in detail below in conjunction with accompanying drawing, but do not limit practical range of the present invention.
Embodiment one:
Present embodiment is a process of utilizing the thermal coupling fixed bed device preparing synthetic gas, and its particular content is as follows:
Take by weighing a certain amount of high temperature resistant reforming catalyst 5 reformer section 13 of packing into, different zones is loaded the catalyzer difference, oxidation zone 4 epimeres filling water conservancy diversion pottery 11, and hypomere loads high temperature resistant catalytic partial oxidation catalyst 6, and structure of reactor is as shown in Figure 1 and Figure 2.During experiment, at first feed hydrogen and oxygen, wherein hydrogen is excessive, lights by portfire, and purpose is rising temperature of reactor and reducing catalyst, and Sweet natural gas is slowly introduced in beginning after 3 hours, strengthens the amount of Sweet natural gas gradually, is adjusted to suitable ratio at last.Reaction begins to run well.
Sweet natural gas and oxygen enter into heat transfer zone 10 through inlet mouth 1 and 9 respectively and carry out preheating, reach more than 600 ℃, be injected to the oxidation zone 4 rapid complete oxidation and the partial oxidation reactions of taking place of reactor then through nozzle 3, emit a large amount of heats, wherein, part heat by interior pipe partition transmits (reactor shown in Figure 1 be delivered to interior manage 12 and outer tube 7 between the reforming catalyst bed, replenish the shortage of heat of follow-up reforming reaction, reactor shown in Figure 2 is delivered to the inner and outer pipes gap and is brought into heat transfer zone by product), and most of heat makes material reach very high temperature, but under the effect of water conservancy diversion pottery 11 and high temperature resistant catalytic partial oxidation catalyst 6, generate the increase of ratio along with synthetic gas, temperature of charge will be reduced to the temperature of reaction that reforming catalyst is allowed, then, the gas that unreacted Sweet natural gas and oxidation zone 4 reactions generate flow into reformer section 13, the carbonic acid gas that complete oxidation generates, reforming reaction takes place and generates synthetic gas (CO and H under the effect of reforming catalyst 5 in water vapour and excessive Sweet natural gas (methane)
2), further improve the synthetic gas yield, last, the high-temperature synthesis gas that reaction generates is by being discharged by air outlet 8 after heat transfer zone 10 heat exchange, unstripped gas (Sweet natural gas and oxygen) and synthetic gas reach the purpose of preheating material gas and quick cooling syngas in heat transfer zone 10 countercurrent flows.
Embodiment two:
Basic embodiment is with example one, and nozzle changes three runners---natural gas feed into, oxygen feeding and water vapour charging, charge ratio can Sweet natural gas/oxygen steam=1/0.5/0.7, owing to added water vapour,, avoided temperature to reduce so oxygen should be more slightly.
The advantage of utilizing this thermal coupling fixed bed device to prepare synthesis gas is:
(1) adopts this thermal coupling fixed bed device can realize effective utilization of heat, reduced energy consumption, substantially realized the self-heating operation.
(2) thermal coupling between zoneofoxidation heat surplus and the reformer section heat deficiency, reduced the focus temperature, alleviated simultaneously the formation of low temperature " cold spot ", and make whole reactor be in a lower operation of temperature (＞1000 ℃) that the conventional reformation reaction unit of ratio is high 100 ℃, improved the receipts rate of synthesis gas.
(3) through the running of long period, catalyst surface and zoneofoxidation carbon deposition quantity are seldom.
(4) experimental result shows, methane conversion be 92.2%, CO selectively be 92.3%, H2 selectively be 83.3%, substantially near thermodynamics balance level.
Claims (8)
1. method of utilizing thermal coupling fixed bed device to produce synthetic gas, it is characterized in that: this method is implemented in following fixed bed device, and it comprises heat transfer zone, oxidation zone, reformer section, thermal insulation layer, nozzle and high pressure resistant metal shell; Described fixed bed device has adopted the concentric type structure, and oxidation zone is positioned at pipe, and reformer section is positioned at inner and outer pipes gap or oxidation zone bottom, and outer tube is outward a thermal insulation layer, and thermal insulation layer is outward high pressure resistant metal shell; Described heat transfer zone is positioned at the top of device, and nozzle is positioned at the oxidation zone top, oxidation zone epimere filling water conservancy diversion pottery, and hypomere loads high temperature resistant catalytic partial oxidation catalyst, and reformer section is loaded high temperature resistant reforming catalyst; Described thermal insulation layer is positioned at outside the outer tube, and thermal insulation layer is outward high pressure resistant metal shell; Described heat transfer zone is positioned at the top of device, and unstripped gas and synthetic gas carry out the adverse current indirect heat exchange at this; Described nozzle is outer mix type nozzle, is installed in the top of oxidation zone.
The described method for preparing synthetic gas comprises: Sweet natural gas and oxygen at first enter heat transfer zone and carry out preheating, be injected to oxidation zone through nozzle then and carry out complete oxidation and partial oxidation reaction, under the effect of water conservancy diversion pottery and high temperature resistant catalytic partial oxidation catalyst, increase the generation ratio of synthetic gas, material (unreacting material and resultant) temperature flow into reformer section after being reduced to the temperature of reaction that reforming catalyst allows, reforming reaction takes place under the effect of reforming catalyst, at last, product synthetic gas (main component CO and H
2) after the quick heat exchange of heat transfer zone, discharge.
2. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described unstripped gas preheating temperature is more than 600 ℃, realizes by the heat transfer zone that is provided with.
3. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described Sweet natural gas is a civil natural gas, can be Sweet natural gas and mixture of steam, oxygen feeding is a pure oxygen, also can be oxygen and mixture of steam, also three kinds of materials can be added respectively.
4. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described reacting is than being 0.45-0.65 at oxygen/Sweet natural gas, the oxidation zone temperature is 1300-2000 ℃, the reformer section temperature is～1000 ℃, and pressure is 0.1-5MPa, and the Sweet natural gas air speed is 1000-1.5 * 10
5h
-1Condition under carry out.
5. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, be provided with portfire in the oxidation zone; This method comprises: at the beginning of the reaction, feed hydrogen and oxygen earlier, hydrogen is excessive, lights by portfire, after 3-8 hour, stops logical hydrogen, increases the amount of Sweet natural gas gradually, just can utilize oxidizing reaction liberated heat self-heating to react.
6. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described fixed bed device oxidation zone top is provided with nozzle, this method comprises: Sweet natural gas after the preheating and oxygen spray into oxidation zone by nozzle respectively through duct separately, and complete oxidation and partial oxidation reaction take place at once.
7. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described heat coupling refers to the coupling of oxidizing reaction with the reforming reaction of heat absorption of heat release, needs the unstripped gas of preheating and needs the coupling of the synthetic gas of fast cooling.
8. according to the method for claims 1 described Sweet natural gas preparing synthetic gas, wherein, described synthetic gas refers to the gas that is applicable to processes such as downstream production methyl alcohol, F-T synthesize, H
2/ CO ratio is 2: 1.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106147865A (en) * | 2016-07-19 | 2016-11-23 | 西安交通大学 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN107673309A (en) * | 2017-09-19 | 2018-02-09 | 北京林业大学 | A kind of method that natural gas prepares synthesis gas with biomass carbon coproduction |
| CN114249299A (en) * | 2021-11-09 | 2022-03-29 | 浦江思欣通科技有限公司 | Pretreatment method of methane-rich gas plasma multiple reforming reaction catalyst |
| CN115253926A (en) * | 2022-07-28 | 2022-11-01 | 中国核动力研究设计院 | Hydrogen and oxygen recombiner |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5278901A (en) * | 1975-12-26 | 1977-07-02 | Mitsui Toatsu Chem Inc | Gacification method |
| CN1191987C (en) * | 2001-11-01 | 2005-03-09 | 中国石油大庆石化分公司研究院 | Method for producing synthesis gas by catalyzing and transforming natural gas and methane |
| CN101597030B (en) * | 2009-07-10 | 2011-06-29 | 清华大学 | Method for preparing H2 and CO synthesis gas by using methane partial oxidation device |
-
2009
- 2009-12-16 CN CN2009102598818A patent/CN101723324B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106147865A (en) * | 2016-07-19 | 2016-11-23 | 西安交通大学 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN106147865B (en) * | 2016-07-19 | 2019-10-01 | 陕西中核交大超洁能源技术有限公司 | The method and apparatus of continuous supercritical water double tube reactor gasification organic matter |
| CN107673309A (en) * | 2017-09-19 | 2018-02-09 | 北京林业大学 | A kind of method that natural gas prepares synthesis gas with biomass carbon coproduction |
| CN114249299A (en) * | 2021-11-09 | 2022-03-29 | 浦江思欣通科技有限公司 | Pretreatment method of methane-rich gas plasma multiple reforming reaction catalyst |
| CN115253926A (en) * | 2022-07-28 | 2022-11-01 | 中国核动力研究设计院 | Hydrogen and oxygen recombiner |
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