CN103183318A - Method for hydrogen production by light hydrocarbon steam reforming in moving bed and device - Google Patents

Abstract

A method and device for producing hydrogen by steam reforming light hydrocarbons in a moving bed, comprising: light hydrocarbons and water vapor enter the reactor from the bottom after being preheated, contact with reforming catalysts and adsorption catalysts with different particle sizes in countercurrent, light hydrocarbons and water vapor are in the Under the condition of steam reforming, H ₂ , CO and CO ₂ are reacted, and CO ₂ reacts with CaO in the adsorption catalyst to convert into CaCO ₃ ; the product gas generated by the reaction is separated from the gas and solid at the top of the reactor and enters the subsequent purification and separation device to obtain high purity. Hydrogen; the mixed catalyst enters the screening separator from the bottom of the reactor and is separated according to particle size. The separated reforming catalyst is returned to the moving bed reactor for recycling, and the separated adsorption catalyst is regenerated and returned to the moving bed reactor for recycling. The method and device provided by the invention eliminate the frequent high-temperature oxidation of the reforming active component Ni to NiO and then reduce it to metal Ni in a reducer, simplify the process, prolong the life of the catalyst and reduce the energy consumption of the system.

Description

A moving bed light hydrocarbon steam reforming hydrogen production method and device

technical field

The present invention relates to a method and device for catalytic conversion of petroleum hydrocarbons, more specifically, to a process method and device for steam reforming of methane to produce hydrogen.

Background technique

The production of clean fuels will inevitably lead to an increase in the demand for hydrogen. Although there are many methods for hydrogen production, the hydrogen production technology using various minerals including coal, oil and natural gas as raw materials is still the most important method. Among them, the most mature and commonly used Hydrocarbon steam reforming is still the hydrogen production process. Natural gas steam reforming (Steam Methane Reforming, SME) is currently the method with the lowest cost and the largest hydrogen production capacity in hydrogen production. About 1/2 of the hydrogen is produced by natural gas steam. Transformation method (SRM) prepared. Hydrogen production by steam reforming of methane mostly uses fixed-bed reactors. In order to reduce the pressure drop of the reactor, the catalyst generally adopts a honeycomb solid catalyst with a particle diameter of Φ(15-20)×(10-15)mm, and the active component is Nickel oxide. The hydrogen production process includes one or two-stage conversion reactions at 800-820°C. The by-product CO is transformed into CO ₂ at 300-450°C in two stages. CO and CO ₂ are further removed by solvent absorption or methanol washing, and the final balanced CO ₂ The gas phase content is 15-20%, and the hydrogen content is less than 75%. Subsequent pressure swing adsorption is used to obtain high-purity industrial hydrogen. Hydrogen production by steam reforming of methane has the characteristics of strong endothermic reversible reaction. In terms of technology, there are disadvantages such as high reaction temperature, low hydrogen concentration, many steps in the reaction and purification process, low production capacity, and large investment. In terms of catalysts, due to the large catalyst particles , there is a gradient in internal heat transfer, and the catalyst has short lifespan and other defects.

CN1903431A discloses a composite catalyst for hydrogen production by steam reforming of methane with adsorption enhancement, which is mainly composed of CaO with calcium carbonate and/or calcium hydroxide powder as the precursor and nickel carbonate , nickel oxide or nickel nitrate as the precursor active nickel component and alumina carrier composite, the molar ratio of each component is, CaO:NiO:Al ₂ O ₃ =1:(0.1-2.0):(0.1-3.0) , the composite catalyst utilizes CaO to remove CO ₂ from the reaction system in time through chemical reaction, and strengthen the steam reforming reaction of methane. In addition, the heat released by the reaction of CaO and _CO2 just compensates for the strong endothermic requirement of hydrogen reforming.

CN1974375A discloses a method for hydrogen production by adsorption-enhanced steam reforming of methane using a fixed-bed reactor. The hydrogen-production reaction and the regeneration of the composite catalyst are carried out simultaneously in different fixed-bed reactors and used alternately. A composite catalyst containing a catalyst and an adsorbent, a fixed-bed reactor and a regenerator system are used to realize a stable and continuous production process of producing high-concentration hydrogen by steam reforming of methane. It can directly and continuously produce hydrogen with a purity of 90-98%. Since the time for the adsorbent to reach adsorption saturation is very short, it is fundamentally difficult to achieve time matching by using this kind of fixed bed alternate switching, and normal operation cannot be carried out.

CN1935634A proposes an adsorption-enhanced methane steam reforming hydrogen production process using a circulating fluidized bed. Adopt the composite catalyst particles containing CaO and active nickel disclosed in CN1903431A, the catalyst particle diameter is 5-200 microns, the active component NiO on the catalyst is reduced to metal Ni; the catalyst after reduction enters the reaction system, under fluidized state , methane and water vapor contact with the catalyst, react to generate H ₂ and CO ₂ , and the generated CO ₂ chemically reacts with CaO on the catalyst, and remains on the catalyst particles in the form of CaCO ₃ . After the reaction is saturated, the catalyst is stripped and then enters the regenerator for high-temperature calcination to decompose CaCO ₃ into CaO and CO ₂ at a high temperature, so that the catalyst can recover its chemical adsorption activity and be recycled. The specific steps are: transport the composite catalyst to the regenerator for pretreatment; the pretreated composite catalyst is then degassed and then reduced in a hydrogen environment; Enter water vapor and methane, the composite catalyst in the fluidized state, methane and water vapor simultaneously carry out reforming hydrogen production reaction, the reaction residence time is 1 second to 5 minutes, the reaction gas velocity is 0.3 ~ 1.0 m/s, the composite catalyst and reaction The ratio of methane is 10:1~0.002:1. After the composite catalyst is used, it is transferred to the regenerator for heating and regeneration, and it can be recycled, which can realize the stability and continuity of the operation of the fluidized bed reactor, and has high mass transfer and heat transfer efficiency. The advantages.

The method disclosed in CN1935634A effectively solves the shortcomings of fixed bed heat transfer and low mass transfer rate through circulating fluidized continuous operation, but the method has the following disadvantages:

1) Due to the use of composite catalysts, Ni, which is the active component of methane steam reforming, is cyclically reduced and oxidized in the reactor and regenerator during the circulating fluidization process, especially the high-temperature regeneration process is likely to cause the sintering of Ni active components and lose live;

2) After the reforming active component Ni is oxidized to NiO in the regenerator, it needs to be reduced to metal Ni in the reducer, and the best state is to reduce it at low temperature to avoid the aggregation of Ni metal particles and inactivation, so that It is necessary to lower the temperature of the regenerated catalyst to carry out the reduction reaction, and the reduced catalyst has to be heated up to the reaction temperature, resulting in a large amount of energy consumption.

Judging from the current situation of hydrogen production by steam reforming of methane, since the development of catalysts for steam reforming of methane is relatively mature, and since hydrogen production by steam reforming of methane is a strong endothermic process, how to reduce the energy consumption of the process has become a process A hotspot for development and innovation.

However, these existing technologies have the defect that the catalyst is frequently burnt and regenerated, which will easily cause the catalyst to destroy its high dispersion due to the growth of Ni grains, affect the activity and stability of the catalyst, and make it difficult for the device to operate stably. How to solve it reasonably Continuous adsorption regeneration of adsorbent in adsorption-enhanced steam reforming is an internationally recognized technical bottleneck in this field.

Contents of the invention

One of the technical problems to be solved by the present invention is to provide a method for producing hydrogen by steam reforming of light hydrocarbons, which can meet the requirements of continuous production. While realizing steam reforming to produce hydrogen, the catalyst activity is stable for a long time, and the internal heat transfer and temperature are stable. control.

The second technical problem to be solved by the present invention is to provide a production device for producing hydrogen by steam reforming of light hydrocarbons with a simple structure.

A method for producing hydrogen by steam reforming of moving bed light hydrocarbons provided by the present invention comprises:

(1) After preheating, light hydrocarbons and water vapor enter the reactor from the bottom, and contact with reforming catalysts and adsorption catalysts with different catalyst particle sizes in countercurrent, and light hydrocarbons and water vapor react under steam reforming conditions to generate H ₂ and CO and CO ₂ , the CO ₂ reacts with the CaO in the adsorption catalyst and converts it into CaCO ₃ ;

(2) The product gas and mixed catalysis in step (1) are gas-solid separated at the top of the reactor, and the separated product gas enters the subsequent purification and separation device to obtain high-purity hydrogen;

(3) The mixed catalyst enters the sieving separator from the bottom of the reactor and is separated according to particle size. The separated reforming catalyst is returned to the reactor for recycling, and the separated adsorption catalyst enters the regenerator for regeneration, and then returns to the reactor for recycling.

A moving bed reaction device for hydrogen production by steam reforming of light hydrocarbons, the device includes a moving bed reactor, a sieving separator, a catalyst riser and a regenerator, the lower part of the moving bed reactor is connected to the sieving separator, and the inside of the sieving separator is The screen is divided into two kinds of catalyst outlets with different particle sizes. One of the catalyst outlets is connected to the bottom of the catalyst riser, and the other outlet is connected to the catalyst regenerator after being sealed. The lower part of the regenerator is connected to the bottom of the catalyst riser after being sealed. The upper part of the riser communicates with the upper part of the moving bed reactor; the upper part of the moving bed reactor is provided with a reaction product outlet through a gas-solid separation device, and the bottom is provided with a light hydrocarbon and steam raw material inlet.

Compared with the prior art, the beneficial effects of the moving bed light hydrocarbon steam reforming hydrogen production method and device provided by the present invention are as follows:

The method provided by the present invention adopts a countercurrent moving bed reactor and two kinds of catalysts with different particle sizes. On the one hand, it strengthens the hydrogen production reaction of methane and water vapor. device, avoiding the oxidation and sintering deactivation of Ni active components caused by the high temperature regeneration process.

The method and device provided by the invention have high conversion efficiency of hydrogen production from light hydrocarbons, stable automatic temperature control, improved heat transfer efficiency, and reasonably solve the bottleneck problem of continuous adsorption and regeneration of adsorbents, making the device and operation more simplified and safe. And the whole device has a simple and compact structure.

Description of drawings

Fig. 1 is a schematic flow diagram of the method and device for hydrogen production by steam reforming of light hydrocarbon moving bed provided by the present invention.

In the figure: 3-moving bed reactor; 5-sieving separator; 11-regenerator; 15-first granular material sealing valve; 16-second granular material sealing valve; 1, 2, 4, 6, 7, 8, 9, 10, 12, 13, 14, 17 are pipelines.

Detailed ways

The method for producing hydrogen by steam reforming of methane provided by the invention is specifically implemented as follows:

(1) After preheating, light hydrocarbons and water vapor enter the reactor from the bottom, and contact with reforming catalysts and adsorption catalysts with different catalyst particle sizes in countercurrent, and light hydrocarbons and water vapor react under steam reforming conditions to generate H ₂ and CO and CO ₂ , the CO ₂ undergoes a chemical adsorption reaction with the adsorption catalyst, and the CaO in the adsorption catalyst is converted into CaCO ₃ ;

(2) The product gas and the mixed catalyst in step (1) are gas-solid separated at the top of the reactor, and the separated product gas enters a subsequent separation and purification device to obtain high-purity hydrogen;

(3) The mixed catalyst enters the sieving separator from the bottom of the reactor and is separated according to particle size. The separated reforming catalyst is returned to the reactor for recycling, and the separated adsorption catalyst enters the regenerator for regeneration, and then returns to the reactor for recycling.

In the method provided by the present invention, the light hydrocarbons are C1-C8 petroleum hydrocarbons, including dry gas, liquefied petroleum gas, and straight-run naphtha produced by various refineries with a distillation range <220°C.

In the method provided by the present invention, the light hydrocarbon and steam are preheated to 350-550°C, preferably 400-450°C, and introduced into the reactor.

In the method provided by the invention, the weight ratio of the light hydrocarbons to water vapor is 1:(1-5), preferably 1:(2-4).

In the method provided by the present invention, the steam reforming conditions are a temperature of 650-860° C., preferably 680-820° C., and a pressure of 0.1-3.0 MPa, preferably 0.15-2.5 MPa.

In the method provided by the present invention, the high-temperature regeneration of the adsorption catalyst is regenerated by transporting air into the regenerator after material sealing, the temperature of the regenerator is 690-1250°C, preferably 720-920°C, and the pressure is 0.1-0.2MPa After the regeneration is completed, the regenerated adsorption catalyst is sealed and returned to the reactor for reuse, and the flow rate of the regenerated adsorption catalyst returned to the reactor is controlled according to the reaction temperature.

In the method provided by the present invention, fuel is preferably added to supplement heat in the regenerator. The heavy fuel oil includes atmospheric heavy oil, vacuum gas oil, coking gas oil, asphalt, atmospheric residue, vacuum residue, coal water slurry, and coal powder.

In the method provided by the present invention, preferably, the steam reforming catalyst is a pellet catalyst with a large particle diameter, and the adsorption catalyst is a pellet catalyst with a small particle diameter. The small particle size means that the adsorption catalyst particle size is smaller than that of the steam reforming catalyst particle size. More preferably, the particle size of the steam reforming catalyst is 2-3 mm, and the average particle size of the adsorbed catalyst particles is 0.1-1 mm.

In the method provided by the invention, the adsorption catalyst is a heat-resistant inorganic oxide catalyst containing calcium carbonate and/or calcium oxide active components. Preferably, the adsorption catalyst is a composite catalyst of calcium oxide and/or calcium carbonate, and alumina. More preferably, based on the total amount of the catalyst, the content of calcium oxide and/or calcium carbonate in the adsorption catalyst is 5-30% by weight, and the content of aluminum oxide is 70-95% by weight.

In the method provided by the invention, the steam reforming catalyst is a heat-resistant inorganic oxide catalyst containing nickel oxide active components. The heat-resistant inorganic oxide is selected from one or a mixture of alumina, silica, zirconia, titania, antimony oxide, iron oxide, copper oxide, magnesium oxide, molybdenum oxide and tungsten oxide. Preferably, the steam reforming catalyst is a nickel oxide/alumina composite catalyst, more preferably, based on the total amount of the catalyst, in terms of oxides, the content of nickel oxide in the steam reforming catalyst is 12- 16% by weight, and the content of alumina is 84 to 88% by weight.

In the method provided by the present invention, the moving bed reactor refers to a reactor used to realize a gas-solid phase reaction process or a liquid-solid phase reaction process. Continuously add granular or massive solid reactants or catalysts at the top of the reactor. As the reaction progresses, the solid materials gradually move down and are finally continuously discharged from the bottom. The fluid then passes through the solid bed from bottom to top, or from top to bottom, to react. Since there is basically no relative movement between the solid particles, but there is a downward movement of the solid particle layer, it can also be regarded as a moving fixed-bed reactor.

A moving bed reaction device for hydrogen production by steam reforming of light hydrocarbons, the device includes a moving bed reactor, a sieving separator, a catalyst riser and a regenerator, the lower part of the moving bed reactor is connected to the sieving separator, and the inside of the sieving separator is The screen is divided into two kinds of catalyst outlets with different particle sizes. One of the catalyst outlets is connected to the bottom of the catalyst riser, and the other outlet is connected to the catalyst regenerator after being sealed. The lower part of the regenerator is connected to the bottom of the catalyst riser after being sealed. The upper part of the riser communicates with the upper part of the moving bed reactor; the upper part of the moving bed reactor is provided with a reaction product outlet through a gas-solid separation device, and the bottom is provided with a light hydrocarbon and steam raw material inlet.

The method provided by the present invention will be described in detail below in conjunction with the accompanying drawings. But the present invention is not limited thereby.

The accompanying drawing is a flow chart of the hydrogen production method of light hydrocarbon moving bed steam reforming provided by the present invention. As shown in the figure, a gas-solid separator is installed at the top of the moving bed reactor 3 for separating solid catalyst and product gas. The separated product gas enters the subsequent hydrogen separation and purification device through the pipeline 4 and then enters the pipe network; the solid catalyst flowing out from the lower part of the moving bed reactor 3 contains two kinds of reforming catalysts and adsorption catalysts with different particle sizes and enters the screening separator 5 , separating two kinds of catalysts with different particle sizes, preferably the steam reforming catalyst is a small spherical catalyst with a large particle size, and the adsorption catalyst is a small spherical catalyst with a small particle size. The reforming catalyst separated by the screening separator 5 enters the bottom of the catalyst lifting pipeline 10 through the catalyst delivery pipeline 6, and returns to the upper part of the moving bed reactor 3 after being lifted by the steam from the pipeline 8; The first material-sealed particle valve 15 for air-locking and pressure-locking enters the delivery pipeline 9 of the standby catalyst, and is transported into the bottom of the regenerator 11 by the air from the pipeline 7, and the supplemented heavy fuel oil enters the lower part of the regenerator 11 through the pipeline 14, and is adsorbed The carbon dioxide adsorption catalyst burns to remove the coke attached to it, and removes the carbon dioxide in the catalyst while increasing the temperature. The high-temperature flue gas at the top of the regenerator is discharged through the pipeline 13, which can be used for heat exchange with water vapor; the adsorption catalyst after burning and heating enters the catalyst through the second material sealing particle valve 16 and the catalyst delivery pipeline 12 for locking gas and pressure The bottom of the lifting pipeline 10 is lifted by the steam from the pipeline 8 and then returned to the upper part of the reactor. The second material sealing particle valve 16 adjusts the flow rate of the adsorption catalyst returning to the moving bed reactor 3 according to the reactor temperature control, so as to realize the control of the reactor temperature. Automatic and stable control; the preheated light hydrocarbon raw material from the pipeline 1 and the water vapor from the pipeline 2 enter the moving bed reactor 3 from the lower part, and contact and react with the two catalysts in the moving bed reactor; the fresh adsorption catalyst can be Supplement enters catalyst delivery pipeline 7 through pipeline 17, and supplementation is carried out under normal pressure. Since the supplementation speed is slow, it will not affect the temperature control of the reactor.

The present invention will be further described below in conjunction with embodiment, but does not limit the present invention thereby.

In an embodiment, the steam reforming catalyst is a nickel oxide/alumina catalyst, and the preparation method is as follows:

Adopt commercially available alumina pellets (industrial products, Aluminum Corporation of China Shandong Aluminum Plant) with a particle diameter of 2 to 3 mm, and use nickel nitrate solution in the ratio of nickel to aluminum even if the catalyst contains 14% by weight of nickel oxide. Immersed for 1 hour, dried at 120°C for 2 hours, and calcined at 1000°C for 2 hours to obtain a steam reforming catalyst. According to analysis, the steam reforming catalyst contains 14% by weight of nickel oxide, 86% by weight of aluminum oxide, the particle size is 2-3 mm, and the apparent bulk density of the catalyst is 0.71 g/ml.

The adsorption catalyst is a calcium oxide/alumina catalyst, and the preparation method is as follows:

Calcium oxide powder (industrial product, Zibo Qilu Ethylene Chemical Co., Ltd.) and alumina powder (industrial product, Aluminum Corporation of China Shandong Aluminum Factory) were kneaded according to the proportion of calcium oxide containing 10% by weight, and rolled on a rolling ball machine Form into pellets with a particle diameter of 0.1-1 mm, dry at 120°C for 4 hours, and then calcinate at 550°C for 2 hours to obtain an adsorption catalyst. The catalyst has an apparent bulk density of 0.75 g/ml, and contains 10% by weight of calcium oxide and 90% by weight of aluminum oxide.

Example

The test process is shown in the attached figure. The desulfurized natural gas is used as the light hydrocarbon raw material (methane content > 96v%, sulfur content < 0.5 μg/g) to be preheated to 400°C, and the water vapor is preheated to 500°C and enters the mobile from the bottom. The bed reactor is in countercurrent contact with the steam reforming catalyst and the adsorption catalyst entering from the upper part of the moving bed reactor, and the steam reforming reaction occurs to generate hydrogen. Catalysts with large particle sizes, steam reforming catalysts with large particle sizes enter the catalyst lifting pipeline and are directly returned to the top of the moving bed reactor after being lifted by steam; adsorption catalysts with small particle sizes enter the catalyst delivery pipeline after passing through the first material sealing particle valve, and are transported by air It is transported into the regenerator, and M100 fuel oil is injected into the regenerator to assist combustion. The temperature of the regenerator is adjusted through the control of the oil volume, and the regenerated flue gas is discharged from the upper part. The temperature of the regenerated adsorption catalyst is raised to 850°C-860°C, and enters the catalyst lifting pipeline through the second material-sealed particle valve, is lifted by steam, and then returns to the moving bed reactor. The second material-sealed particle valve adjusts the flow rate of the catalyst so that the The bed temperature was maintained at 780°C.

The pressure of the moving bed reactor is 0.5MPa, the bed temperature is 780°C, the pressure of the regenerator is 0.1MPa, and the temperature is controlled at 850°C-860°C. The volume space velocity of product hydrogen relative to the moving bed reactor is 1000h ^-1 , the weight ratio of natural gas and water vapor is 1:2.5, the conversion rate of methane in natural gas after reaction is >90%, and the product gas contains 68-70v% hydrogen , sent to the latter membrane separator for separation to obtain 90-92v% medium-purity hydrogen, or sent to a pressure swing adsorption separation device to obtain higher-purity 99.9999v% high-purity hydrogen.

Claims (20)

1. a moving-bed lighter hydrocarbons producing hydrogen from steam conversion method is characterized in that, comprising:

(1) enter reactor by the bottom after lighter hydrocarbons and the water vapour preheating, the steam reforming catalyst different with the granules of catalyst particle diameter and adsorptive catalyst counter current contact, lighter hydrocarbons and water vapour react under the steam reformation condition and generate H ₂, CO and CO ₂, described CO ₂Be converted into CaCO with the CaO reaction in the adsorptive catalyst ₃

(2) product gas in the step (1) and mixed catalyst are in the reactor head gas solid separation, and separated products gas enters the later separation purifying plant and obtains high-purity hydrogen;

(3) mixed catalyst enters the screening separator by reactor bottom and separates by particle diameter, recycles in the isolated reforming catalyst Returning reactor, and isolated adsorptive catalyst enters revivifier regeneration, recycles in the Returning reactor then.

2. according to the method for claim 1, it is characterized in that described lighter hydrocarbons are the petroleum hydrocarbon of C1～C8.

3. according to the method for claim 1, it is characterized in that the weight ratio of described lighter hydrocarbons and water vapour is 1: (1～5).

4. according to the method for claim 3, it is characterized in that the weight ratio of described lighter hydrocarbons and water vapour is 1: (2～4).

5. according to the method for claim 1, it is characterized in that described lighter hydrocarbons and water vapour are preheated to 350～550 ℃ and introduce in the reactor.

6. according to the method for claim 5, it is characterized in that described lighter hydrocarbons and water vapour are preheated to 400～450 ℃ and introduce in the reactor.

7. according to the method for claim 1, it is characterized in that described steam reformation condition is: temperature is 650～860 ℃, and pressure is 0.1～3.0MPa.

8. according to the method for claim 7, it is characterized in that described steam reformation condition is: temperature is 680～820 ℃, and pressure is 0.15～2.5MPa.

9. according to the method for claim 1, it is characterized in that described steam reforming catalyst is the heat-resistant inorganic oxide catalyzer that contains the nickel oxide active ingredient.

10. according to the method for claim 9, it is characterized in that described steam reforming catalyst is nickel oxide/aluminum oxide composite catalyst.

11. the method according to claim 10 is characterized in that, is benchmark with the total catalyst weight, in oxide compound, the content of nickel oxide is 12～16 heavy % in the described steam reforming catalyst, and the content of aluminum oxide is 84～88 heavy %.

12. the method according to claim 1 is characterized in that, described adsorptive catalyst is the heat-resistant inorganic oxide catalyzer that contains calcium carbonate and/or calcium oxide active ingredient.

13. the method according to claim 12 is characterized in that, described adsorptive catalyst is the composite catalyst of calcium oxide and/or calcium carbonate and aluminum oxide.

14. the method according to claim 13 is characterized in that, is benchmark with the total catalyst weight, in oxide compound, the content of calcium oxide and/or calcium carbonate is 5～30 heavy % in the described adsorptive catalyst, and the content of aluminum oxide is 70～95 heavy %.

15. the method according to claim 1 is characterized in that, described adsorptive catalyst is honored as a queen through material and is delivered in the revivifier 690～1250 ℃ of regeneration down by air.

16. the method according to claim 15 is characterized in that, adsorptive catalyst is regenerated under 720～920 ℃ condition in the described revivifier.

17. the method according to claim 15 or 16 is characterized in that, adds the fuel refreshment heat in the described revivifier.

18. the method according to claim 1 is characterized in that, the steam reforming catalyst described in the step (1) is big particle diameter pellet catalyst, and described adsorptive catalyst is the small particle size pellet catalyst.

19. the method according to claim 18 is characterized in that, the grain diameter of described steam reforming catalyst is 2～3 millimeters, and the grain diameter of described adsorptive catalyst is 0.1～1 millimeter.

20. lighter hydrocarbons producing hydrogen from steam conversion moving bed reaction device, it is characterized in that, this device comprises moving-burden bed reactor, the screening separator, catalyzer riser tube and revivifier, the moving-burden bed reactor bottom is communicated with the screening separator, screening separator inside is divided into the catalyst outlet of two kinds of different-grain diameters through screen cloth, one of them catalyst outlet is communicated with catalyzer riser tube bottom, another outlet is through the material connection catalyst regenerator of being honored as a queen, be honored as a queen through material and be communicated with catalyzer riser tube bottom in the revivifier bottom, catalyzer riser tube top is communicated with moving-burden bed reactor top; Described moving-burden bed reactor top arranges reacting product outlet through gas-solid separation equipment, and the bottom arranges lighter hydrocarbons and water vapour feed(raw material)inlet.

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