CN106006555A - System and method for preparing hydrogen-rich gas and calcium carbide - Google Patents
System and method for preparing hydrogen-rich gas and calcium carbide Download PDFInfo
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- CN106006555A CN106006555A CN201610592316.3A CN201610592316A CN106006555A CN 106006555 A CN106006555 A CN 106006555A CN 201610592316 A CN201610592316 A CN 201610592316A CN 106006555 A CN106006555 A CN 106006555A
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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Abstract
The invention relates to a system and a method for preparing hydrogen-rich gas and calcium carbide. The system comprises a mixing forming unit, a high-temperature pyrolysis unit, a catalytic reforming unit, a transformation and decarbonization unit and a calcium carbide smelting unit, wherein the mixing forming unit comprises a coal dust inlet, a calcium-based raw material inlet, an adhesive inlet and a briquette outlet; the high-temperature pyrolysis unit comprises a briquette inlet, a raw gas outlet and a high-temperature active pellet outlet; the catalytic reforming unit comprises a raw gas inlet and a synthetic gas outlet; the transformation and decarbonization unit comprises a synthetic gas inlet and a hydrogen-rich gas outlet; the calcium carbide smelting unit comprises a high-temperature active pellet inlet and a calcium carbide outlet. The method for preparing the hydrogen-rich gas and the calcium carbide by virtue of the system comprises the following steps: performing mixing forming and pyrolysis on coal dust and a calcium-based raw material to obtain raw gas, and performing catalytic reforming, transformation and decarbonization to obtain the hydrogen-rich gas; smelting obtained high-temperature active pellets to obtain the calcium carbide. According to the system and the method, the heat of pyrolysis gas is utilized, and the pyrolysis gas with complex components is also transformed into the hydrogen-rich gas.
Description
Technical field
The invention mainly relates to the production field of carbide, particularly relate to a kind of hydrogen-rich gas and carbide prepared
System and method.
Background technology
At present, after low-order coal in powdery and quick lime are raw material pressure ball, then through being pyrolyzed to obtain high temperature active
Pelletizing is the most industrially verified with the technique preparing carbide.This technique is at conservation cost and carries
High thermal efficiency aspect all achieves important breakthrough.But, in the process, although after pyrolysis, high temperature is lived
Property pelletizing heat utilized, and be pyrolyzed after the amount of heat entrained by raw coke oven gas at follow-up point
It is cooled during from and slatterns.Additionally, in the carbide acetylene chemical process of subsequent development, carbide
React with water, produce substantial amounts of carbide slag (main component is calcium hydroxide), if can not get effectively utilizing
Not only result in the wasting of resources, also surrounding can be made a very bad impression.
Meanwhile, containing substantial amounts of methane and carbon monoxide in the pyrolysis gas that pyrolysis of coal produces, and methane water steams
Gas is reformed and CO shift reaction is the most industrial more ripe containing methane and carbon monoxide gas system
The method of hydrogen-rich gas, its dominant response includes that methane and steam react to obtain carbon monoxide and hydrogen,
And carbon monoxide reacts carbon dioxide processed and hydrogen with steam.In view of type ball high temperature pyrolysis gained
The temperature of pyrolysis gas is close with methane-steam reforming, if by the methane in pyrolysis gas and an oxidation
Carbon is converted into hydrogen by steam reforming reaction and transformationreation, then pyrolysis gas can become rich H2 gas
Body.
It addition, because being required to steam in methane vapor reforming and carbon monoxide transformation process, because of
This can add part carbide slag in the quick lime as carbide raw materials for production.So can not only be by electricity
Calcium oxide in rock ballast becomes raw material, reduces cost of material, moreover it is possible to the water in carbide slag is become equally
For the raw material of pyrolysis gas high-temperature catalytic reaction, the step that carbide slag slurries is dried and calcines can be saved, enter one
Step saves energy consumption.
Therefore, for the problems referred to above, it is necessary to invent and a kind of prepare hydrogen-rich gas and the system of carbide and side
Method, it is possible to make full use of pyrolysis gas.
Summary of the invention
For the problems referred to above, prepare hydrogen-rich gas and the system of carbide and side it is desirable to provide a kind of
Method, the problem of pyrolysis gas waste when the purpose of this system and method is to solve to produce carbide.Further,
The present invention also can reduce the cost of carbide raw material, makes full use of carbide slag.
The system preparing hydrogen-rich gas and carbide that the present invention provides includes: mixed-forming unit, high temperature
Pyrolysis unit, catalytic reforming units, conversion, decarburization unit and carbide smelt unit, wherein, institute
State mixed-forming unit and include coal powder entrance, calcio feed(raw material)inlet, binding agent entrance and the outlet of type ball,
Mixed-forming for type ball；Described high temperature pyrolysis unit includes the outlet of type ball entrance, raw coke oven gas and height
Temperature activity pelletizing outlet, for the pyrolysis of type ball；Described type ball entrance and described mixed-forming unit
The outlet of type ball is connected；Described catalytic reforming units includes raw coke oven gas entrance and syngas outlet, for first
Alkane and the catalytic reforming of steam；Described raw coke oven gas entrance goes out with the raw coke oven gas of described high temperature pyrolysis unit
Mouth is connected；Described conversion, decarburization unit include synthesis gas entrance and hydrogen-rich gas outlet, for an oxygen
Change the catalytic shift reaction of carbon and the carbonization treatment generating gas；Described synthesis gas entrance and described catalysis
The syngas outlet of reformer unit is connected；Described carbide smelt unit include high temperature active pelletizing entrance and
Carbide exports, for smelting high temperature active pelletizing for carbide；Described high temperature active pelletizing entrance and institute
The high temperature active pelletizing outlet stating high temperature pyrolysis unit is connected.
Above-mentioned system, described catalytic reforming units is reforming reactor, inside it the most successively
It is provided with filter course, the catalyst layer of catalytic cracking of tar, the catalyst layer of methane reforming.
Above-mentioned system, described conversion, decarburization unit include change furnace, are provided with inside described change furnace
Transformation catalyst layer.
Above-mentioned system, described system may also include heat-insulation conveying device, described heat-insulation conveying device with
Described carbide smelts high temperature active pelletizing entrance and the high temperature active ball of described high temperature pyrolysis unit of unit
Group's outlet is connected.
Further, in above-mentioned system, described mixed-forming unit includes mixing arrangement and molding dress
Put, in described mixing arrangement, be provided with blender；Described shaped device includes the mixed material sequentially arranged
Warehouse and to squeezing double rollers；The mixed material entrance of described mixed material warehouse is mixed with described mixing arrangement
Conjunction material outlet is connected.
Further, described system may also include material processing unit, and described material processing unit includes
Coal breaker, the middle warehouse of coal and the pulverized coal screw conveying device being sequentially connected, and be sequentially connected
Calcio raw material breaker, warehouse, calcio raw material powder helix transporting device in the middle of calcio raw material.
The present invention also provides for a kind of method utilizing said system to prepare hydrogen-rich gas and carbide, including with
Lower step: < < the calcio raw material of 3mm and binding agent are described mixed for the coal dust of 1mm, particle diameter by particle diameter
After being mixed into mixed material in synthesis type unit, re-compacted molding ball；Described type ball is sent into described height
Temperature pyrolysis unit is pyrolyzed, and obtains raw coke oven gas and high temperature active pelletizing；Described raw coke oven gas is sent into institute
State catalytic reforming units, obtain synthesis gas through filtration, catalytic cracking of tar and methyl hydride catalyzed reformation；
Described synthesis gas is sent into described conversion, decarburization unit carries out transformationreation so that in described synthesis gas
Carbon monoxide be converted into hydrogen and carbon dioxide, then after decarburization, prepare hydrogen-rich gas；By described height
Temperature activity pelletizing is sent into described carbide and is smelted unit, smelts and prepares carbide.
Above-mentioned method, the addition of described binding agent is the 1.0wt%-10.0wt% of described mixed material；
Described calcio raw material includes that carbide slag and quick lime, the addition of described carbide slag are described quick lime
20wt%-40wt%；Described calcio raw material is 1.0-1.5:1 with the addition mass ratio of described coal dust.
In said method, the temperature of described catalytic reforming is 750-920 DEG C, and pressure is 2-3MPa；Described
The temperature of transformationreation is 200-320 DEG C, and the catalyst of described transformationreation is Co-Mo system resistant to sulfur width temperature
Catalyst.
Above-mentioned method, described method may further comprise the step of: sends into described raw material by coal with calcio raw material
Processing unit so that coal is crushed to that < 1mm becomes coal dust so that described calcio raw material is crushed to < 3mm；
Described coal is middle or low price coal.
Technical scheme so that carry the steam of high temperature with pyrolysis gas at catalytic reforming reaction
In device and change furnace after catalytic reaction, finally give hydrogen-rich gas, on the one hand can make full use of pyrolysis
The heat of gas, on the other hand can be converted into hydrogen-rich gas by the pyrolysis gas of complicated component.
The present invention can also be used with part carbide slag and substitutes calcium oxide so that carbide slag is turned waste into wealth, and without
Through carbonization and calcining step, reduce cost of material.Meanwhile, calcium hydroxide is utilized to decompose generation
Steam and the methane in pyrolysis gas and reaction of carbon monoxide, steam owing to calcium hydroxide decomposes the water produced
Gas is more, it is possible to reduce the carbon distribution of catalyst, extends the life-span of catalyst.
Further, the present invention is pyrolyzed the high temperature active pelletizing of generation and can be incubated and be transported to furnace of calcium carbide,
Improve the efficiency of utilization of system.
Accompanying drawing explanation
Fig. 1 is the system flow chart preparing hydrogen-rich gas and carbide of the embodiment of the present invention；
Fig. 2 is the system structure schematic diagram preparing hydrogen-rich gas and carbide of the embodiment of the present invention.
Detailed description of the invention
As in figure 2 it is shown, system for producing calcium carbide described in the invention by material processing unit 1, be mixed into
Type unit 2, high temperature pyrolysis unit 3, catalytic reforming units 4, conversion, decarburization unit 5 and carbide
Smelt unit 6 to form.
In order to reduce cost of material and give full play to the effect of native system, the coal in the present invention is middle low order
Fine coal.
Material processing unit 1 is for crush feed coal and Calx or carbide slag, and it includes that coal is broken
Warehouse 14 in the middle of warehouse 13, calcio raw material in the middle of device 11, calcio raw material breaker 12, coal,
Pulverized coal screw conveying device 15 and calcio raw material powder helix transporting device 16.Described breaker successively with
Middle warehouse helix transporting device is connected.The most in the present invention, material processing unit 1 is not necessary to
Arrange, can decide whether to arrange according to supplied materials size.
Mixed-forming unit 2 is used for the mixing to raw material and molding, including mixing arrangement and shaped device.
Mixing arrangement is high intensity mixer, is provided with coal powder entrance 21, calcio feed(raw material)inlet 22, binding agent enter
Mouth 23, blender 24 and mixed material outlet 25.Described coal powder entrance 21, calcio feed(raw material)inlet
22 are connected with the helix transporting device 15 and 16 of material processing unit 1 respectively.Shaped device includes mixing
Compound material warehouse 26 and to squeezing double rollers 27.Described warehouse 26 entrance is connected with mixed material outlet 25.
The device of high temperature pyrolysis unit 3 is preheating furnace, for being pyrolyzed type ball, enters including type ball
Mouth 31, raw coke oven gas outlet 32 and high temperature active pelletizing outlet 33.Described type ball entrance 31 can pass through
Crowded double roller outlets 27 (i.e. type ball outlet) are connected by helix transporting device with mixed-forming unit 2.
The device of catalytic reforming units 4 is reforming reactor, for being steamed with water by the methane in pyrolysis gas
Gas carries out catalytic reforming reaction, is provided with raw coke oven gas entrance 41 and syngas outlet 46.Described raw coke oven gas enters
Mouth 41 exports 32 with the raw coke oven gas of high temperature pyrolysis unit 3 and is connected.It is provided with inside described reforming reactor
Gas distributor 42 and the filter course 43 being arranged in order from the bottom up, catalytic cracking of tar catalyst
Layer 44, methane reforming catalyst layer 45.Gas distributor 42 is used for allowing gas to the most more uniform leading to
Cross catalyst layer.Described filter course can be ceramic filter plate, it is therefore an objective to remove the dust in raw coke oven gas also
Play the effect of accumulation of heat.The purpose of described catalytic cracking of tar catalyst is to be filled by the tar in raw coke oven gas
Divide catalysis to obtain pyrolysis gas.The purpose of described reforming catalyst layer be methane during catalytic thermal is vented one's spleen with
Steam reacts, and methane is converted to hydrogen and carbon monoxide.
Conversion, the device of decarburization unit 5 include change furnace and absorption unit of dioxide carbon, for an oxygen
Change the transformationreation of carbon and generate the carbonization treatment of gas, with prepared hydrogen-rich gas, being provided with synthesis gas and enter
Mouth 51 and hydrogen-rich gas outlet 54.Described synthesis gas entrance and the syngas outlet of catalytic reforming units 4
46 are connected.Gas distributor 52 and transformation catalyst layer 53 it is provided with inside described change furnace.Gas divides
Being disposed to of cloth device 52 allows gas to the most more uniform pass through catalyst layer.Transformation catalyst layer 53
Purpose be that catalytic CO carries out transformationreation, generate carbon dioxide enriched and hydrogen.Again through dioxy
After carbon dioxide sloughed by change carbon absorption plant, hydrogen rich gas can be prepared.
It is furnace of calcium carbide that carbide smelts the device of unit 6, for high temperature active pelletizing smelting pyrolysis produced
Refining is carbide, is provided with high temperature active pelletizing entrance 61, calcium carbide furnace gas outlet 62 and carbide outlet 63.
Described high temperature active pelletizing entrance 61 can be by the high temperature active of heat-insulation conveying device with high temperature pyrolysis unit
Pelletizing outlet 33 is connected.Described high temperature conveyer device can be the one in heat-preserving container or insulation carrier bar.
High temperature conveyer device is set and can further improve the efficiency of utilization of system.
As it is shown in figure 1, the present invention utilizes the method that said system prepares hydrogen-rich gas and carbide, including
Following steps:
The first step: pretreatment of raw material, is i.e. crushed to < 1mm, calcio by breaker by middle low-order coal
Raw material is crushed to < 3mm；Certainly this step is not necessary to arrange, concrete depending on supplied materials size；
Second step: mixed-forming, mixes coal dust, calcio raw material and binding agent, and compressing；
The addition of binding agent is mixed material 1.0wt%-10.0wt%；The addition of carbide slag is quick lime
20wt%-40wt%；Calcio raw material is 1.0-1.5:1 with the addition mass ratio of coal dust；
3rd step: type ball high temperature pyrolysis, will send into preheating furnace heat by helix transporting device by institute's die mould ball
Solve, obtain raw coke oven gas and high temperature active pelletizing；Wherein, pyrolysis temperature is 800-1100 DEG C, during pyrolysis
Between can be 15-45min；Wherein helix transporting device nor is it necessary that setting；
4th step: catalytic reforming, pyrolysis raw coke oven gas enters catalytic reforming units, and through filtering, tar is urged
Change cracking and methyl hydride catalyzed reformation obtains synthesis gas；Wherein, the temperature of catalytic reforming units is
750-920℃；Pressure is 2-3MPa；
5th step: catalytic shift, decarburization, the synthesis gas after catalytic reforming, anti-further across conversion
Should, convert carbon monoxide to hydrogen and carbon dioxide, then hydrogen-rich gas can be obtained after decarburization；Conversion
The temperature of reaction is 200-320 DEG C, and used catalyst is Co-Mo system resistant to sulfur width temperature catalyst；
6th step: high temperature active pelletizing processes, and high temperature active pelletizing is warm is transported to furnace of calcium carbide, at electricity
It is heated to 1800-2200 DEG C in stone stove, smelts and prepare liquid carbide and calcium carbide furnace gas.
According to the technique scheme of the present invention, by heavy in catalysis with pyrolysis gas for the steam carrying high temperature
In whole reactor and change furnace after catalytic reaction, finally give hydrogen-rich gas, on the one hand can be fully sharp
With the heat of pyrolysis gas, on the other hand the pyrolysis gas of complicated component can be converted into hydrogen-rich gas.Enter
One step, the present invention can also be used with part carbide slag and substitutes calcium oxide so that carbide slag is turned waste into wealth, and nothing
Cost of material need to be reduced through carbonization and calcining step.Meanwhile, utilize calcium hydroxide to decompose to produce
Steam and pyrolysis gas in methane and reaction of carbon monoxide, owing to calcium hydroxide decomposes the water produced
Steam is more, it is possible to reduce the carbon distribution of catalyst, extends the life-span of catalyst.
As expansion, the carbide obtained and water also can be reacted generation acetylene and carbide slag, electricity by the present invention
Again can be as raw material after rock ballast is purified, system can form closed cycle.
Further, the present invention is pyrolyzed the high temperature active pelletizing of generation and can be incubated and be transported to furnace of calcium carbide,
Further increase efficiency of utilization.
" wt% " herein refers both to percentage by weight.
Embodiment 1
With jet coal and add 30wt% carbide slag quick lime as raw material, first pass through broken milling device
Raw coal size is crushed to that < 1mm, calcio raw material granularity is crushed to < 3mm；Then coal dust is former with calcio
Material powder and binding agent powder mix with the mass ratio of 1.0:1.0:0.22, at 15Mpa after stirring further
Under pressure compressing；Type ball warp helix transporting device is pyrolyzed 30min in delivering to preheating furnace at 900 DEG C,
Obtain raw coke oven gas and high temperature active pelletizing.It is anti-that raw coke oven gas is at high temperature fed directly to catalytic reforming conversion
Answering device, keeping reactor temperature is 850 DEG C, and pressure is 2MPa, raw coke oven gas sequentially pass through purifying and dedusting,
Obtaining synthesis gas after catalytic cracking of tar reaction, synthesis gas is transported in change furnace catalysis at 320 DEG C and becomes
After changing, finally make pyrolysis gas composition based on carbon dioxide and hydrogen, the most again through decarburization, obtain
Rich H to high concentration2Gas；High temperature active pelletizing is sent in furnace of calcium carbide through sealed thermal insulating conveying equipment,
Smelt at 2000 DEG C and obtain carbide；Follow-up carbide can obtain a large amount of carbide slag, after purification after reacting with water
Can be recycled for use as the raw material that carbide produces.
Embodiment 2
With jet coal and add 20wt% carbide slag quick lime as raw material, first pass through broken milling device
Raw coal size is crushed to that < 1mm, calcio raw material granularity is crushed to < 3mm；Then coal dust is former with calcio
Material powder and binding agent powder mix with the mass ratio of 1.0:1.5:0.025, after stirring further
Under 15Mpa pressure compressing；Type ball warp helix transporting device is pyrolyzed in delivering to preheating furnace at 900 DEG C
30min, it is thus achieved that raw coke oven gas and high temperature active pelletizing.Raw coke oven gas is at high temperature fed directly to catalytic reforming
Conversion reactor, keeping reactor temperature is 750 DEG C, and pressure is 3MPa, and raw coke oven gas sequentially passes through only
Obtaining synthesis gas after eliminating dirt, catalytic cracking of tar reaction, synthesis gas is transported in change furnace 260 DEG C
After lower catalytic shift, finally make pyrolysis gas composition based on carbon dioxide and hydrogen, pass through the most again
Decarburization, obtains the rich H of high concentration2Gas；High temperature active pelletizing sends into electricity through sealed thermal insulating conveying equipment
In stone stove, smelt at 2000 DEG C and obtain carbide；Follow-up carbide can obtain a large amount of carbide slag after reacting with water,
The raw material that carbide produces is can be recycled for use as after purification.
Embodiment 3
With jet coal and add 40wt% carbide slag quick lime as raw material, first pass through broken milling device
Raw coal size is crushed to that < 1mm, calcio raw material granularity is crushed to < 3mm；Then coal dust is former with calcio
Material powder and binding agent powder mix with the mass ratio of 1.0:1.25:0.12, after stirring further
Under 15Mpa pressure compressing；Type ball warp helix transporting device is pyrolyzed in delivering to preheating furnace at 900 DEG C
30min, it is thus achieved that raw coke oven gas and high temperature active pelletizing.Raw coke oven gas is at high temperature fed directly to catalytic reforming
Conversion reactor, keeping reactor temperature is 920 DEG C, and pressure is 2.5MPa, and raw coke oven gas sequentially passes through
Obtaining synthesis gas after the reaction of purifying and dedusting, catalytic cracking of tar, synthesis gas is transported in change furnace 200 DEG C
After lower catalytic shift, finally make pyrolysis gas composition based on carbon dioxide and hydrogen, pass through the most again
Decarburization, obtains the rich H of high concentration2Gas；High temperature active pelletizing sends into electricity through sealed thermal insulating conveying equipment
In stone stove, smelt at 2000 DEG C and obtain carbide；Follow-up carbide can obtain a large amount of carbide slag after reacting with water,
The raw material that carbide produces is can be recycled for use as after purification.
As seen from the above-described embodiment, technical scheme solves pyrolysis gas waste when producing carbide
Problem.Further, the present invention also can reduce the cost of carbide raw material, makes full use of carbide slag.
Last it is noted that obvious, above-described embodiment is only by clearly demonstrating what the present invention was made
Citing, and not restriction to embodiment.For those of ordinary skill in the field, exist
Can also make other changes in different forms on the basis of described above.Here without also without
All of embodiment is given exhaustive by method.And the obvious change thus amplified out or variation
Among protection scope of the present invention.
Claims (10)
1. preparing a system for hydrogen-rich gas and carbide, described system includes mixed-forming unit, height
Temperature pyrolysis unit, catalytic reforming units, conversion, decarburization unit and carbide smelting unit, wherein,
Described mixed-forming unit includes coal powder entrance, calcio feed(raw material)inlet, binding agent entrance and type ball
Outlet, for the mixed-forming of type ball；
Described high temperature pyrolysis unit includes the outlet of type ball entrance, raw coke oven gas and the outlet of high temperature active pelletizing,
Pyrolysis for type ball；Described type ball entrance exports with the type ball of described mixed-forming unit and is connected；
Described catalytic reforming units includes raw coke oven gas entrance and syngas outlet, for methane and steam
Catalytic reforming；Described raw coke oven gas entrance exports with the raw coke oven gas of described high temperature pyrolysis unit and is connected；
Described conversion, decarburization unit include synthesis gas entrance and hydrogen-rich gas outlet, for carbon monoxide
Catalytic shift reaction with generate gas carbonization treatment；Described synthesis gas entrance and described catalytic reforming
The syngas outlet of unit is connected；
Described carbide is smelted unit and is included high temperature active pelletizing entrance and carbide outlet, for being lived by high temperature
Property pelletizing smelt for carbide；Described high temperature active pelletizing entrance is alive with the high temperature of described high temperature pyrolysis unit
Property pelletizing outlet be connected.
System the most according to claim 1, it is characterised in that described catalytic reforming units is attached most importance to
Whole reactor, be sequentially provided with from the bottom up inside it filter course, the catalyst layer of catalytic cracking of tar,
The catalyst layer of methane reforming.
System the most according to claim 1, it is characterised in that described conversion, decarburization unit bag
Include change furnace, inside described change furnace, be provided with transformation catalyst layer.
System the most according to claim 1, it is characterised in that described system also includes being incubated defeated
Device, described heat-insulation conveying device and described carbide is sent to smelt high temperature active pelletizing entrance and the institute of unit
The high temperature active pelletizing outlet stating high temperature pyrolysis unit is connected.
System the most according to claim 1, it is characterised in that described mixed-forming unit includes
Mixing arrangement and shaped device, be provided with blender in described mixing arrangement；Described shaped device includes depending on
Mixed material warehouse that sequence is arranged and to squeezing double rollers；The mixed material entrance of described mixed material warehouse with
The mixed material outlet of described mixing arrangement is connected.
System the most according to claim 1, it is characterised in that described system also includes at raw material
Reason unit, described material processing unit includes coal breaker, the middle warehouse of coal and the coal being sequentially connected
Powder helix transporting device, and be sequentially connected calcio raw material breaker, warehouse in the middle of calcio raw material,
Calcio raw material powder helix transporting device.
7. one kind utilizes the side that system described in any one of claim 1 to 6 prepares hydrogen-rich gas and carbide
Method, comprises the following steps:
By particle diameter, < < calcio raw material and the binding agent of 3mm are mixed into described for the coal dust of 1mm, particle diameter
After being mixed into mixed material in type unit, re-compacted molding ball；
The described type ball described high temperature pyrolysis unit of feeding is pyrolyzed, obtains raw coke oven gas and high temperature active
Pelletizing；
Described raw coke oven gas is sent into described catalytic reforming units, through filtration, catalytic cracking of tar and first
Alkane catalytic reforming obtains synthesis gas；
Described synthesis gas is sent into described conversion, decarburization unit carries out transformationreation so that described synthesis
Carbon monoxide in gas is converted into hydrogen and carbon dioxide, then prepares hydrogen-rich gas after decarburization；
Described high temperature active pelletizing is sent into described carbide and smelts unit, smelt and prepare carbide.
Method the most according to claim 7, it is characterised in that the addition of described binding agent is
The 1.0wt%-10.0wt% of described mixed material；Described calcio raw material includes carbide slag and quick lime, institute
State the 20wt%-40wt% that addition is described quick lime of carbide slag；Described calcio raw material and described coal dust
Addition mass ratio be 1.0-1.5:1.
Method the most according to claim 7, it is characterised in that the temperature of described catalytic reforming is
750-920 DEG C, pressure is 2-3MPa；The temperature of described transformationreation is 200-320 DEG C, described conversion
The catalyst of reaction is Co-Mo system resistant to sulfur width temperature catalyst.
Method the most according to claim 7, it is characterised in that described method further comprises the steps of:
Coal and calcio raw material are sent into described material processing unit so that coal be crushed to < 1mm becomes coal dust,
Described calcio raw material is made to be crushed to < 3mm；Described coal is middle low-order coal.
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