CN204737928U - System for hot desulfurization of circulating fluidized bed dry process production synthetic natural gas or coproduction hydrogen manufacturing uses coordinately - Google Patents
System for hot desulfurization of circulating fluidized bed dry process production synthetic natural gas or coproduction hydrogen manufacturing uses coordinately Download PDFInfo
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- CN204737928U CN204737928U CN201520433668.5U CN201520433668U CN204737928U CN 204737928 U CN204737928 U CN 204737928U CN 201520433668 U CN201520433668 U CN 201520433668U CN 204737928 U CN204737928 U CN 204737928U
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Abstract
The utility model discloses a system for hot desulfurization of circulating fluidized bed dry process production synthetic natural gas or coproduction hydrogen manufacturing uses coordinately, it includes that quench washing device, circulating fluidized bed hot method desulphurization unit, smart desulfurization protection bed device, the non - converting means of nai sulphur, adsorption bed take off NH3HCN device and SNG product gas apparatus for producing to can increase by a hydrogen plant. The utility model discloses a hot desulfurization of circulating fluidized bed dry process combines effective appropriate allocation of the resistant sulphur transform of non - and methanation, hydrogen manufacturing technique, make full use of the heat of above -mentioned reaction, produce the qualified hydrogen product of qualified SNG product or coproduction production.
Description
Technical field
The device of the crude synthesis gas production synthetic natural gas that the gasification that the utility model relates to coal or other carbonaceous material produces or coproduction hydrogen manufacturing.In particular to the flow process configuration of a kind of production synthetic natural gas in conjunction with circulating fluidized bed dry thermally desulfurizing and non-sulfur-resisting transformation technology or coproduction hydrogen manufacturing, relate to a kind of system being combined circulating fluidized bed dry desulfurization production synthetic natural gas or coproduction hydrogen manufacturing more specifically.
Background technology
Existing take coal as the technology of raw material production synthetic natural gas and industrial practice in, usually adopt gasification to produce crude synthesis gas, crude synthesis gas regulates (H through sulfur-tolerant water gas shift and liquid phase scrubbing method desulfurization and decarburization technology
2-CO
2)/(CO+CO
2) value about 3.0, enter methanation reaction device.
Current use more widely liquid phase scrubbing method desulfurization and decarburization technology has Rectisol technique and Selexol technique, wherein:
Rectisol technique adopts methyl alcohol to be lyosorption, operates at very low temperature, need consume a large amount of cold.
Use Polyethylene glycol dimethyl ether for solvent in Selexol technique, but this technique has certain difficulty to the COS removed in synthetic gas, as COS high for concentration in sour gas removed, COS hydrolysis unit need be increased, and the internal circulating load of solvent causes greatly running cost high.
Carry out the high-temperature synthesis gas of autopneumatolysis after sulfur-tolerant water gas shift, temperature is usually at 270-450 DEG C, and above liquid phase scrubbing method desulfurization and decarburization technology is invalid in such high-temperature gas, because these methods typically need to operate at the temperature that sub-zero zero is lower, therefore synthetic gas needs to carry out recovery of heat process, to meet the cold condition of liquid phase scrubbing method desulfurization and decarburization technology removing impurity, and decontaminating syngas temperature after desulfurization and decarburization is lower, do not reach the light-off temperature 230-300 DEG C required for methanation reaction.Thus enter methanator to need with extra heat by the temperature needed for unstripped gas re-heat to methanation, whole flow process heat arranges unreasonable, there is malaria, and thermo-efficiency utilizes and reduces.
Synthetic gas methanation reaction belongs to strong exothermal reaction, and the CO methanation of every 1% can produce the thermal insulation warming of 74 DEG C, every CO of 1%
2methanation can produce the thermal insulation warming of 60 DEG C.And the temperature of the methanation catalyst of industrial application is generally at 230-750 DEG C, be subject to the restriction of catalyzer service temperature, therefore need the temperature rise effectively controlling methanation reaction.
Current methanation device both domestic and external adopts circulation methanation process to control temperature of reaction mostly, as Lurgi methanation process adopts three methanators, wherein the first two methanator adopts series-parallel system to connect, main employing part second methanator gas product is as circulation gas, control the first methanator bed temperature, first methanator temperature out is 650 DEG C, and the second methanator temperature out is 500-650 DEG C.
Davy methanation process adopts four methanators, wherein the first two methanator adopts series-parallel system to connect, main employing part second methanator gas product is as circulation gas, control the first methanator bed temperature, first, second methanator temperature out is 620 DEG C.
Top's rope methanation process adopts five methanators, the first two methanator adopts series-parallel system to connect, adopt part first methanator gas product as circulation gas, control the first methanator bed temperature, first, second reactor outlet temperature is 675 DEG C.
There is following shortcoming in above-mentioned circulation methanation process:
(1) owing to using recycle compressor, device fabrication difficulty, invests high, and the energy consumption of synthesis loop increases.
(2) adopt circulation gas to control the temperature of methanation reaction general higher, there is the possibility of temperature runaway, easily cause catalyzer high temperature sintering.
(3) temperature due to methanation is higher, causes methanator to need quite thick refractory liner, is unfavorable for the installation and removal of reactor and easily occurs the damage of lining.
(4) temperature out due to methanator is too high, makes follow-up heat-exchange equipment and pipeline have higher temperature tolerance, thus adds cost of investment.
Utility model content
The utility model removes the sulfocompound of synthetic gas by the hot method of circulating fluidized bed, the shortcoming adopting above-mentioned liquid phase scrubbing method desulfurization to exist can be avoided, synthetic gas after desulfurization partly or entirely keeps synthetic gas in higher temperature (exceeding the light-off temperature of methanation catalyst) through non-sulfur-resisting transformation, enters into methanation reaction device and/or device for producing hydrogen.Regulated the composition of crude synthesis gas by non-sulfur-resisting transformation, make to enter CO in the synthetic gas of methanation device
2increase with the concentration of water vapor, effectively control the temperature rise of methanation reaction.
Methanation device in the utility model adopts loop-free methanation process, do not need to arrange recycle gas compressor, and methanator temperature out is lower than the reactor outlet temperature of conventional high-temperature circulation methanation process, reactor and follow-up workshop section equipment material cost are effectively reduced.The synthetic gas going out methanation device finally enters decarbonation device and drying installation, obtains qualified synthetic natural gas product.
The utility model is for the production of coproduction hydrogen manufacturing all right while synthetic natural gas.Through the synthetic gas of non-sulfur-resisting transformation, enter after adsorption bed removes NH3/HCN, all or part of demethanization reaction unit production synthetic natural gas, part goes device for producing hydrogen to produce hydrogen in addition.
Based on above-mentioned thinking, the purpose of this utility model aims to provide a kind of system being combined circulating fluidized bed dry thermally desulfurizing production synthetic natural gas or coproduction hydrogen manufacturing.The method removes the sulfocompound of crude synthesis gas by the hot method desulfurization of circulating fluidized bed, and the synthetic gas then after desulfurization is partially or completely through the CO of non-sulfur resistant conversion process adjustment crude synthesis gas, H
2, CO
2with the composition of water vapor, and in heat recuperation, solid dry removal crude synthesis gas other impurity such as NH3 and HCN, all or part of purification conversion synthetic gas enters the methanation device without circulation process, by tolerance, the CO converted in synthetic gas of the desulfurized syngas without non-sulfur-resisting transformation
2the temperature rise of methanator is regulated with water vapor.The synthetic gas going out methanation device removes remaining CO finally by decarbonation device
2, then enter drying installation dehydration, produce qualified SNG.Partial cleansing conversion synthetic gas enters the non-sulfur-resisting transformation device of low temperature to carry out depth conversion and obtains hydrogen-rich gas, and hydrogen-rich gas enters PSA purification section after heat recuperation to carry out PSA decarbonation and carries hydrogen, produces qualified hydrogen.The method configures liquid phase scrubbing method desulfurization and decarburization and produces the low problem of the synthetic gas heat utilization ratio that exists in SNG or coproduction process for making hydrogen after can solving traditional sulfur resistant conversion process.
Technical problem to be solved in the utility model can be achieved through the following technical solutions:
Be combined the system of the method for circulating fluidized bed dry thermally desulfurizing production synthetic natural gas or coproduction hydrogen manufacturing, it comprises:
Quench washing device, described Quench washing device has a crude synthesis gas input aperture and the first crude synthesis gas delivery port, and described crude synthesis gas input aperture is connected by pipeline with the crude synthesis gas delivery port of a crude synthesis gas forming apparatus;
The hot method desulfurizer of circulating fluidized bed, described circulating fluidized bed hot method desulfurizer has one first crude synthesis gas input aperture and high temperature desulfurizing syngas outlet and rich SO
2pneumatic outlet, described first crude synthesis gas input aperture is connected by pipeline with the first crude synthesis gas delivery port of described Quench washing device; Described rich SO
2pneumatic outlet sends rich SO
2gas is to sulfuric acid production plant or sulphur production installation;
Fine de-sulfur protection bed apparatus, described fine de-sulfur protection bed apparatus has high temperature desulfurizing synthetic gas entrance and the outlet of at least one high-temperature fine desulfurized syngas, and described high temperature desulfurizing synthetic gas entrance is connected by the high temperature desulfurizing syngas outlet of the hot method desulfurizer of pipeline and described circulating fluidized bed;
Non-sulfur-resisting transformation device, described non-sulfur-resisting transformation device has high-temperature fine desulfurized syngas entrance and conversion syngas outlet, and described high-temperature fine desulfurized syngas entrance is protected the high-temperature fine desulfurized syngas of bed apparatus to export by pipeline and described fine de-sulfur to be connected;
Adsorption bed takes off NH
3/ HCN device, described adsorption bed takes off NH
3/ HCN device has conversion synthetic gas entrance and at least one removing impurities conversion syngas outlet, and described conversion synthetic gas entrance is connected by the conversion syngas outlet of pipeline with described non-sulfur-resisting transformation device;
SNG gas product production equipment, described SNG gas product production equipment has removing impurities conversion synthetic gas entrance and SNG product gas outlet, and the removing impurities conversion synthetic gas entrance of described SNG gas product production equipment takes off NH by pipeline and described adsorption bed
3the removing impurities conversion syngas outlet of/HCN device connects, and described SNG product gas outlet sends SNG gas product.
In a preferred embodiment of the present utility model, described adsorption bed takes off NH
3the conversion synthetic gas entrance of/HCN device is also protected the high-temperature fine desulfurized syngas in bed apparatus to export by a high-temperature fine desulfurized syngas line of pipes with described fine de-sulfur to be connected.
In a preferred embodiment of the present utility model, described adsorption bed takes off NH
3/ HCN device has two removing impurities conversion syngas outlet, be divided into the first removing impurities conversion syngas outlet and the second removing impurities conversion syngas outlet, wherein the first removing impurities conversion syngas outlet is converted synthetic gas entrance with the described removing impurities in described SNG gas product production equipment and is connected by pipeline; Describedly realize the above-mentioned system being combined the method for circulating fluidized bed dry thermally desulfurizing production synthetic natural gas or coproduction hydrogen manufacturing and also comprise a device for producing hydrogen, described device for producing hydrogen also has removing impurities conversion synthetic gas entrance and hydrogen outlet, and the removing impurities conversion synthetic gas entrance of described device for producing hydrogen takes off NH by pipeline and described adsorption bed
3second removing impurities conversion syngas outlet of/HCN device connects.
In a preferred embodiment of the present utility model, the pipeline between the outlet of high-temperature fine desulfurized syngas and the high-temperature fine desulfurized syngas entrance of described non-sulfur-resisting transformation device of described fine de-sulfur protection bed apparatus is also connected with a water vapour and supplements and manage.
In a preferred embodiment of the present utility model, described SNG gas product production equipment comprises:
First methanation reaction device, described first methanation reaction device has removing impurities conversion synthetic gas entrance and the outlet of the first methanation reaction gas, and the removing impurities conversion synthetic gas entrance of described first methanation reaction device takes off NH by pipeline and described adsorption bed
3removing impurities conversion syngas outlet in/HCN device or the first removing impurities conversion syngas outlet connect;
Second heat reclaim unit, described second heat reclaim unit has the first methanation reaction gas entrance and the outlet of the second methanation reaction gas, and described first methanation reaction gas entrance is exported with the first methanation reaction gas in described first methanation reaction device and is connected by pipeline;
Second methanation reaction device, described second methanation reaction device has the second methanation reaction gas entrance and the outlet of front three alkanisation reaction gas, described second methanation reaction gas entrance to be exported with the second methanation reaction gas of described second heat reclaim unit by pipeline and is connected, and described second methanation reaction gas entrance also takes off NH by a removing impurities conversion synthetic gas line of pipes and described adsorption bed
3removing impurities conversion syngas outlet in/HCN device or the first removing impurities conversion syngas outlet connect;
3rd heat reclaim unit, described 3rd heat reclaim unit has front three alkanisation reaction gas entrance and the outlet of the 4th methanation reaction gas, and described front three alkanisation reaction gas entrance is exported with the front three alkanisation reaction gas of described second methanation reaction device and is connected by pipeline;
Front three alkanisation reaction unit, described front three alkanisation reaction unit has the 4th methanation reaction gas entrance and the outlet of the 5th methanation reaction gas, and described 4th methane reaction gas entrance to be exported with the 4th methanation reaction gas of described 3rd heat reclaim unit by pipeline and is connected;
4th heat reclaim unit, described 4th heat reclaim unit has the 5th methanation reaction gas entrance and the first methane rich syngas outlet, and described 5th methanation reaction gas entrance to be exported with the 5th methanation reaction gas of described front three alkanisation reaction unit by pipeline and is connected;
Second refrigerating unit, described second refrigerating unit has the first methane rich synthetic gas entrance and the second methane rich syngas outlet, and described first methane rich synthetic gas entrance is connected by the first methane rich syngas outlet of pipeline with described 4th heat reclaim unit;
CO2 removal device, described CO2 removal device has the second methane rich synthetic gas entrance and SNG product gas outlet, described second methane rich synthetic gas entrance is connected with the second methane rich syngas outlet of described second refrigerating unit by pipeline, and described SNG product gas outlet sends SNG gas product.
In a preferred embodiment of the present utility model, also comprise a drying and dehydrating device, described drying installation has SNG gas product entrance and dried SNG product gas outlet, and the SNG gas product entrance of described drying and dehydrating device is connected with the SNG product gas outlet in described CO2 removal device by pipeline; The dried SNG product gas outlet of described drying and dehydrating device sends dried SNG gas product.
In a preferred embodiment of the present utility model, described first methanation reaction device is conveying bed methanation reaction device or adiabatic methanation reaction unit.
In a preferred embodiment of the present utility model, described second methanation reaction device is adiabatic methanation reaction unit.
In a preferred embodiment of the present utility model, described front three alkanisation reaction unit is isothermal methanation reaction unit.
In a preferred embodiment of the present utility model, described CO2 removal device is PSA decarbonation device or MDEA decarbonation device.
In a preferred embodiment of the present utility model, described drying and dehydrating device is TEG dehydration device.
In a preferred embodiment of the present utility model, described device for producing hydrogen comprises:
The non-sulfur-resisting transformation device of low temperature, the non-sulfur-resisting transformation device of described low temperature has removing impurities conversion synthetic gas entrance and the first low temperature shift syngas outlet, and the removing impurities conversion synthetic gas entrance of described low temperature non-sulfur-resisting transformation device takes off NH by pipeline and described adsorption bed
3the second removing impurities conversion syngas outlet in/HCN device connects;
First heat reclaim unit, described first heat reclaim unit has the first low temperature shift synthetic gas entrance and the second low temperature shift syngas outlet, and described first low temperature shift synthetic gas entrance is connected by pipeline with the first low temperature shift syngas outlet of the non-sulfur-resisting transformation device of described low temperature;
First refrigerating unit, described first refrigerating unit has the second low temperature shift synthetic gas entrance and the 3rd low temperature shift syngas outlet, and described second low temperature shift synthetic gas entrance is connected by pipeline with the second low temperature shift syngas outlet of described first heat reclaim unit;
Refining plant, described refining plant has the 3rd low temperature shift synthetic gas entrance and hydrogen outlet, and described 3rd low temperature shift synthetic gas entrance is connected by pipeline with the 3rd low temperature shift syngas outlet of described first refrigerating unit; Described hydrogen outlet sends qualified hydrogen.
In a preferred embodiment of the present utility model, described refining plant is PSA refining plant.
In a preferred embodiment of the present utility model, described crude synthesis gas forming apparatus is coal water slurry gasifying device or gasifying powder coal device.
Owing to have employed technical scheme as above, the utility model has following characteristics:
1. the utility model is used for producing qualified SNG product or coproduction hydrogen manufacturing.
2. crude synthesis gas do not need to be cooled to after Quench washing required for traditional liquid phase scrubbing method sulfur removal technology lower than the temperature of 40 DEG C, but enter circulating fluidized bed dry thermally desulfurizing device with higher temperature.
3. the temperature of the high-temperature synthesis gas after circulating fluidized bed dry thermally desulfurizing meets the service temperature of fine de-sulfur protection bed, therefore directly can enter fine de-sulfur protection bed.
4. the desulfurized syngas temperature after fine de-sulfur protection bed meets the temperature of non-sulfur-resisting transformation device needs; therefore directly can enter non-sulfur-resisting transformation device, avoiding synthetic gas after using traditional liquid phase scrubbing method desulfurization needs the heating installation used through temperature raising.
5. the desulfurized syngas going out non-sulfur-resisting transformation system still enters adsorption bed with higher temperature and takes off NH
3/ HCN device, avoids adopting traditional water wash column to remove NH3/HCN and the heat waste that causes.
6. go out adsorption bed and take off NH
3the all or part of methanation device that enters of removing impurities conversion synthetic gas of/HCN device is for the production of methane-rich gas, and part enters device for producing hydrogen for the production of hydrogen.
7. go out adsorption bed and take off NH
3the removing impurities conversion synthetic gas of/HCN device directly enters methanation device or the non-sulfur-tolerant water gas shift device of low temperature without the need to heat exchange.
8. methanation device is arranged on adsorption bed and takes off NH
3between/HCN device and decarbonation device, the water vapor amount allocated into before can entering the flow of non-sulfur-resisting transformation operation and non-sulfur-resisting transformation operation by high-temperature fine desulfurized syngas effectively controls the temperature rise of methanator.
9. methanation device of the present utility model does not need to adopt the mode of recycle compressor to control the temperature of methanation reaction, avoids the recycle compressor adopting structure, cost of investment and running cost high, makes the flow process of methanation process simplify greatly simultaneously.
10. the form that first and second methanation reaction device in methanation device adopts series-parallel connection to combine, front three alkanisation reaction unit is isothermal methanation reactor, can improve the transformation efficiency of methanation reaction.
11. the utility model methanation devices can adopt domestic methanation catalyst.
The first methanation reaction device in 12. methanation devices can adopt insulation fix bed reactor or conveying fluid bed reaction apparatus; Adopt conveying fluid bed reaction apparatus, make to carry out methanation reaction continuously in fluidized-bed, improve the throughput of methanation device, adopt transport bed reactor simultaneously, efficient gas solid transfer efficiency can be realized, realize the equal control to methanation reaction temperature, avoid the shortcoming that the pressure drop of traditional fixed bed methanator is larger, effectively reduce the power waste of methanation device.
13. use the utility model to produce SNG or coproduction hydrogen manufacturing, maintain the superior calorific value of the synthetic gas that gasification produces, avoid synthetic gas downstream and utilize additional heat again, effectively improve the thermo-efficiency of synthetic gas.
14. use the utility model to produce SNG or coproduction hydrogen manufacturing, and device process gas capacity is large.
15. the utility model technical process are simple, and equipment takes up an area little, less investment.
16. use the utility model to produce SNG or coproduction hydrogen manufacturing, synthetic gas imurity-removal flow process uses the water content consumption in the flow process of liquid phase scrubbing method decontaminating syngas significantly to reduce than tradition, decrease the pollution of impurity composition to water simultaneously, thus reach the object reducing discharge of wastewater.
The utility model feature is compared with prior art as follows:
1. go for the purification of the crude synthesis gas that various kinds of coal gas mode is produced, such as coal water slurry gasification, coal gasification.
2. at crude synthesis gas configuration cycles fluidized-bed dry method thermally desulfurizing device after Quench washing.
3. fine de-sulfur protection bed is set after circulating fluidized bed dry thermally desulfurizing at crude synthesis gas.
4. after fine de-sulfur protection bed, arrange non-sulfur-resisting transformation device at crude synthesis gas, after can avoiding using traditional liquid phase scrubbing method desulfurization, synthetic gas needs the heating installation used through temperature raising.
5. the transformation catalyst in non-sulfur-tolerant water gas shift technique selects Fe-Cr series catalysts or Cu-Zn series catalysts.
6. at desulfurized syngas, adsorption bed is set after non-sulfur-resisting transformation device and takes off NH
3/ HCN device, avoids adopting traditional water wash column to remove NH3/HCN and the heat waste that causes.
7. synthetic gas after the conversion takes off NH through adsorption bed
3after/HCN device, methanation device is set.Methanation device is arranged on adsorption bed and takes off NH
3between/HCN device and decarbonation device, the water vapor amount allocated into before can entering the flow of non-sulfur-resisting transformation operation and non-sulfur-resisting transformation operation by high-temperature fine desulfurized syngas effectively controls the temperature rise of methanation reaction.
8. synthetic gas after the conversion takes off NH through adsorption bed
3while methanation device is set after/HCN device, can device for producing hydrogen be set, for the production of coproduction hydrogen manufacturing during synthetic natural gas.
9. methanation device does not need to adopt the mode of recycle compressor to control the temperature of methanation reaction, and the flow process of methanation workshop section is simplified greatly.
10. the form that first and second methanation reaction device in methanation device adopts series-parallel connection to combine, front three alkanisation reaction unit is isothermal methanation reactor, can improve the transformation efficiency of methanation reaction.
11. methanation devices can adopt domestic methanation catalyst.
12. first methanation reaction devices can adopt insulation fix bed reactor or conveying fluid bed reaction apparatus.Adopt conveying fluid bed reaction apparatus, make to carry out methanation reaction continuously in fluidized-bed, improve the throughput of methanation device, adopt transport bed reactor simultaneously, efficient gas solid transfer efficiency can be realized, realize the equal control to methanation reaction temperature, avoid the shortcoming that the pressure drop of traditional fixed bed methanator is larger, effectively reduce the power waste of methanation device.
Adopt the non-sulfur-tolerant water gas shift device of low temperature in 13. device for producing hydrogen, depth conversion is carried out to synthetic gas, hydrogen rich gas processed.
14. the utility model produce SNG or coproduction hydrogen manufacturing, maintain the superior calorific value of the synthetic gas that gasification produces, avoid synthetic gas downstream and utilize additional heat again, effectively improve the thermo-efficiency of synthetic gas.
15. the utility model produce SNG or coproduction hydrogen manufacturing, synthetic gas imurity-removal flow process uses the water content consumption in the flow process of liquid phase scrubbing method decontaminating syngas significantly to reduce than tradition, decrease the pollution of impurity composition to water simultaneously, thus reach the object reducing discharge of wastewater.
16. the utility model technical process are simple, and equipment takes up an area little, less investment.
To sum up, the utility model is mainly by the non-sulfur-resisting transformation of circulating fluidized bed dry thermally desulfurizing combine with technique and methanation technology production synthetic natural gas or coproduction hydrogen manufacturing.This technique passes through the heat of reasonable disposition circulating fluidized bed desulfur and non-sulfur-tolerant water gas shift system, remove the sulfocompound in synthetic gas, arsenic and compound thereof, methyl seleninic acid, remove ammonia in synthetic gas and prussiate by ADSORPTION IN A FIXED BED agent, realize the purification of synthetic gas.The conversion synthetic gas of all or part of purification, by the gas of methanation device production methane rich, obtains qualified synthetic natural gas product finally by decarbonation device and drying installation.Conversion synthetic gas Partial cleansing in addition enters the non-sulfur-resisting transformation device of low temperature to carry out depth conversion and obtains hydrogen-rich gas, and hydrogen-rich gas enters PSA purification section after heat recuperation to carry out PSA decarbonation and carries hydrogen, produces qualified hydrogen.
The utility model is by adopting the circulating fluidized bed dry non-sulfur-resisting transformation of thermally desulfurizing combine with technique and methanation technology production synthetic natural gas technique or coproduction hydrogen manufacturing, can Appropriate application heat, simple flow, minimizing equipment, thus effectively save occupation area of equipment and reduce the cost of investment of producing synthesis of natural device of air and coproduction device for producing hydrogen.
The utility model, by the effective and reasonable configuration of circulating fluidized bed dry thermally desulfurizing in conjunction with non-sulfur-resisting transformation and methanation, hydrogen producing technology, takes full advantage of the heat of above-mentioned reaction, produces qualified SNG product or qualified hydrogen product is produced in coproduction.
Accompanying drawing explanation
Fig. 1 is the principle schematic being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of the utility model embodiment 1.
Fig. 2 is the principle schematic being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of the utility model embodiment 2.
Fig. 3 is the principle schematic being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of the utility model embodiment 3.
Fig. 4 is the principle schematic being combined the system of circulating fluidized bed dry desulfurization production synthetic natural gas and co-producing hydrogen of the utility model embodiment 4.
Embodiment
Embodiment 1
See Fig. 1; be combined circulating fluidized bed dry desulfurization production synthetic natural gas system shown in figure, comprise Quench washing device 100, circulating fluidized bed hot method desulfurizer 200, fine de-sulfur protection bed apparatus 300, non-sulfur-resisting transformation device 400, adsorption bed take off NH
3/ HCN device 500, SNG gas product production equipment, MDEA decarbonation device 600, TEG dehydration device 700.SNG gas product production equipment comprise adiabatic methanation reactor 810,820, isothermal methanation reactor 830, heat reclaim unit 840,850,860 and refrigerating unit 870.
The crude synthesis gas input aperture 110 of Quench washing device 100 is connected with the crude synthesis gas delivery port 910 of coal water slurry gasifying device 900 by pipeline 1.
The crude synthesis gas input aperture 210 of the hot method desulfurizer 200 of circulating fluidized bed is connected with the crude synthesis gas delivery port 120 of Quench washing device 100 by pipeline 2.
The rich SO of circulating fluidized bed hot method desulfurizer 200
2pneumatic outlet 220 sends rich SO
2gas produces sulfuric acid or sulphur to the sulfuric acid production plant in downstream or sulphur production installation (not shown).
The high temperature desulfurizing synthetic gas entrance 310 of fine de-sulfur protection bed apparatus 300 is connected by the high temperature desulfurizing syngas outlet 230 of the hot method desulfurizer 200 of pipeline 3 and circulating fluidized bed.
The high-temperature fine desulfurized syngas entrance 410 of non-sulfur-resisting transformation device 400 is protected the high-temperature fine desulfurized syngas of bed apparatus 300 to export 320 by pipeline 4 with fine de-sulfur to be connected.Pipeline 4 is also connected with water vapor and makes up line 5.
Adsorption bed takes off NH
3the conversion synthetic gas entrance 510 of/HCN device 500 is connected by the conversion syngas outlet 420 of pipeline 6 with non-sulfur-resisting transformation device 400.
Adsorption bed takes off NH
3the removing impurities conversion syngas outlet 520 out two femoral canal lines 7 and 8 of/HCN device 500, pipeline 7 converts synthetic gas entrance 811 with the removing impurities of adiabatic methanation reactor 810 and is connected, and the methanation reaction gas outlet 812 of adiabatic methanation reactor 810 is connected with the methanation reaction gas entrance 841 of heat reclaim unit 540 by pipeline 9.
The methanation reaction gas outlet 842 of heat reclaim unit 840 is connected with the methanation reaction gas entrance 821 of adiabatic methanation reactor 820 by pipeline 10.Pipeline 10 is also connected with pipeline 8.
The methanation reaction gas outlet 822 of adiabatic methanation reactor 820 is connected with the methanation reaction gas entrance 851 of heat reclaim unit 850 by pipeline 11.
The methanation reaction gas outlet 852 of heat reclaim unit 850 is connected with the methanation reaction gas entrance 831 of isothermal methane reactor 830 by pipeline 12.
The methanation reaction gas outlet 832 of isothermal methane reactor 830 is connected with the methanation reaction gas entrance 861 of heat reclaim unit 860 by pipeline 13.
The methane rich syngas outlet 862 of heat reclaim unit 860 is connected with the methane rich synthetic gas entrance 871 of refrigerating unit 870 by pipeline 14.
The methane rich syngas outlet 872 of refrigerating unit 870 is connected with the methane rich synthetic gas entrance 610 of MDEA decarbonation device 600 by pipeline 15.
The SNG product gas outlet 620 of MDEA decarbonation device 600 is connected with the SNG gas product entrance 710 of TEG dehydration device 700 by pipeline 16, and the dried SNG product gas outlet 720 of TEG dehydration device 700 sends dried SNG gas product.
This embodiment to be combined circulating fluidized bed dry desulfurization production synthetic natural gas system work process as follows:
Coal water slurry produces in crude synthesis gas through coal water slurry gasifying device 900 sulfocompound H2S and COS, and the impurity such as ammonia and prussiate.Crude synthesis gas is after Quench washing device 100 washs, and temperature is 220-240 DEG C.This crude synthesis gas enters circulating fluidized bed dry thermally desulfurizing device 200.Sulfur-containing impurities in crude synthesis gas is by reacting with the active metal oxide MO in the sorbent material in the desulphurization reactor in circulating fluidized bed dry thermally desulfurizing device 200, and produce the sorbent material MS being loaded with sulphur, M is the metal be present in solid adsorbent.Such as Zn.
In high-temperature synthesis gas after desulfurization, sulphur content can be reduced to 0.1-5ppmv, and temperature is 170-300 DEG C, enters fine de-sulfur protection bed apparatus 300.
In the regeneration reactor of the sorbent material MS being loaded with sulphur in circulating fluidized bed dry thermally desulfurizing device 200 and O
2carry out chemical reaction, the sorbent material MS being loaded with sulphur is regenerated, reaction generates SO
2.Rich SO
2gas temperature is 200-550 DEG C, enters downstream and goes to produce sulfuric acid or sulphur.
High temperature desulfurizing synthetic gas is by after fine de-sulfur protection bed apparatus 300, and sulphur content is reduced to <0.1ppm.Synthetic gas after fine de-sulfur enters non-sulfur-resisting transformation device 400.In non-sulfur-resisting transformation device 400, desulfurized syngas generation transformationreation, the temperature of synthetic gas increases to 250-550 DEG C.Conversion synthetic gas enters adsorption bed and takes off NH3/HCN device 500 after temperature is down to 230-300 DEG C after reclaiming heat in non-sulfur-resisting transformation device 400, removes the NH3/HCN in conversion synthetic gas by ADSORPTION IN A FIXED BED agent.
Conversion synthetic gas after imurity-removal is divided into two strands, and major part wherein enters the adiabatic methanation reactor 810 of the methanation unit in SNG gas product production equipment, in adiabatic methanation reactor 810, and most CO, part CO in synthetic gas
2and H
2reaction generates methane.Go out the synthetic gas temperature of adiabatic methanation reactor 810 at 540 DEG C-600 DEG C, its temperature is by the CO in the water vapor amount allocated into before non-sulfur-resisting transformation device 400 and conversion synthetic gas
2concentration control and regulate.
After adiabatic methanation reactor 810 methanation reaction, gas temperature after heat reclaim unit 840 is reduced to 250-300 DEG C, enters adiabatic methanation reactor 820 after mixing with other one of the conversion synthetic gas after imurity-removal.Continue methanation reaction occurs in adiabatic methanation reactor 820, the Outlet Gas Temperature of adiabatic methanation reactor 820 is at 350 DEG C-550 DEG C, and its temperature is regulated by the conversion synthetic gas tolerance of the imurity-removal entering adiabatic methanation reactor 820.
After adiabatic methanation reactor 820 methanation reaction, gas temperature after heat reclaim unit 850 is reduced to 240-280 DEG C, enters isothermal methanation reactor 830.Continue methanation reaction occurs in isothermal methanation reactor 830, the Outlet Gas Temperature of isothermal methanation reactor 830 is at 250 DEG C-300 DEG C, after heat reclaim unit 860, methane rich synthetic gas temperature is reduced to 100-150 DEG C, and after refrigerating unit 870 cools, temperature is down to 30-75 DEG C.Methane rich synthetic gas after cooling enters MDEA decarbonation device 600, to remove the carbonic acid gas in synthetic gas, then enters TEG dehydration device 700 and removes water in synthetic gas, finally obtain SNG gas product.
Embodiment 2
See Fig. 2, the circulating fluidized bed dry desulfurization production synthetic natural gas system that is combined shown in figure and embodiment 1 to be combined circulating fluidized bed dry desulfurization production synthetic natural gas system substantially identical, high-temperature fine desulfurized syngas after its difference is fine de-sulfur protection bed is divided into two strands, and one is connected with 410 high-temperature fine desulfurized syngas entrances of non-sulfur-resisting transformation 400 device by pipeline 4; Another stock is connected with pipeline 6 by pipeline 4a.And occur in methanation battery limit (BL) methanation reaction use catalyzer active ingredient Ni content and other compositions different from embodiment 1.
This embodiment to be combined circulating fluidized bed dry desulfurization production synthetic natural gas system work process as follows:
Coal water slurry produces in crude synthesis gas through coal water slurry gasifying device 900 sulfocompound H2S and COS, and the impurity such as ammonia and prussiate.Crude synthesis gas is after Quench washing device 100 washs, and temperature is 220-240 DEG C.This crude synthesis gas enters circulating fluidized bed dry thermally desulfurizing device 200.Sulfur-containing impurities in crude synthesis gas is by reacting with the active metal oxide MO in the sorbent material in the desulphurization reactor in circulating fluidized bed dry thermally desulfurizing device 200, and produce the sorbent material MS being loaded with sulphur, M is the metal be present in solid adsorbent.Such as Zn.
In high-temperature synthesis gas after desulfurization, sulphur content can be reduced to 0.1-5ppmv, and temperature is 170-300 DEG C, enters fine de-sulfur protection bed apparatus 300.
In the regeneration reactor of the sorbent material MS being loaded with sulphur in circulating fluidized bed dry thermally desulfurizing device 200 and O
2carry out chemical reaction, the sorbent material MS being loaded with sulphur is regenerated, reaction generates SO
2.Rich SO
2gas temperature is 200-550 DEG C, enters downstream and goes to produce sulfuric acid or sulphur.
High temperature desulfurizing synthetic gas is by after fine de-sulfur protection bed apparatus 300, and sulphur content is reduced to <0.1ppm.Synthetic gas after fine de-sulfur is divided into two strands, and a part of synthetic gas enters non-sulfur-resisting transformation device 400.In non-sulfur-resisting transformation device 400, desulfurized syngas generation transformationreation, the temperature of synthetic gas increases to 250-550 DEG C.After conversion synthetic gas mixes without the synthetic gas converted with another strand after fine de-sulfur after in non-sulfur-resisting transformation device 400, after reclaiming heat, temperature is down to 230-300 DEG C, enter adsorption bed together and take off NH3/HCN device 500, remove the NH3/HCN in conversion synthetic gas by ADSORPTION IN A FIXED BED agent.
Conversion synthetic gas after imurity-removal is divided into two strands, and major part wherein enters the adiabatic methanation reactor 810 of the methanation unit in SNG gas product production equipment, in adiabatic methanation reactor 810, and most CO, part CO in synthetic gas
2and H
2reaction generates methane.Go out the synthetic gas temperature of adiabatic methanation reactor 810 at 540 DEG C-600 DEG C, its temperature is by the CO in the water vapor amount allocated into before non-sulfur-resisting transformation device 400, conversion synthetic gas
2and control without the high-temperature fine desulfurized syngas flow of non-sulfur-resisting transformation device 400 and regulate.
After adiabatic methanation reactor 810 methanation reaction, gas temperature after heat reclaim unit 840 is reduced to 250-300 DEG C, enters adiabatic methanation reactor 820 after mixing with other one of the conversion synthetic gas after imurity-removal.Continue methanation reaction occurs in adiabatic methanation reactor 820, the Outlet Gas Temperature of adiabatic methanation reactor 820 is at 350 DEG C-550 DEG C, and its temperature is regulated by the conversion synthetic gas tolerance of the imurity-removal entering adiabatic methanation reactor 820.
After adiabatic methanation reactor 820 methanation reaction, gas temperature after heat reclaim unit 850 is reduced to 240-280 DEG C, enters isothermal methanation reactor 830.Continue methanation reaction occurs in isothermal methanation reactor 830, the Outlet Gas Temperature of isothermal methanation reactor 830 is at 250 DEG C-300 DEG C, after heat reclaim unit 860, methane rich synthetic gas temperature is reduced to 100-150 DEG C, and after refrigerating unit 870 cools, temperature is down to 30-75 DEG C.Methane rich synthetic gas after cooling enters MDEA decarbonation device 600, to remove the carbonic acid gas in synthetic gas, then enters TEG dehydration device 700 and removes water in synthetic gas, finally obtain SNG gas product.
Embodiment 3
See Fig. 3, the circulating fluidized bed dry desulfurization production synthetic natural gas system that is combined shown in figure and embodiment 2 to be combined circulating fluidized bed dry desulfurization production synthetic natural gas system substantially identical, its difference is just to substitute MDEA decarbonation device 600 with PSA decarbonation device 600a and the SNG product gas outlet 620a cancelling TEG dehydration device 700, PSA decarbonation device 600a directly sends SNG gas product.With the adiabatic methanation reactor 810 in conveying bed methane reaction device 810a alternative embodiment 1, adsorption bed takes off NH
3the removing impurities conversion syngas outlet 520 out two femoral canal line 7a and 8 of/HCN device 500, pipeline 7a converts synthetic gas entrance 811a with the removing impurities of conveying bed methane reaction device 810a and is connected, and the methanation reaction gas outlet 812a of conveying bed methane reaction device 810a is connected with the methanation reaction gas entrance 841 of heat reclaim unit 840 by pipeline 9a.
The crude synthesis gas input aperture 110 of Quench washing device 100 is connected with the crude synthesis gas delivery port 910a of powder coal gasification furnace 900a by pipeline 1a.
The methane rich syngas outlet 872 of refrigerating unit 870 is connected with the methane rich synthetic gas entrance 610a of PSA decarbonation device 600a by pipeline 15a.
The working process being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of this embodiment is as follows:
Fine coal produces thick synthetic gas through powder coal gasification furnace 900a, and after Quench washing device 100 washs, temperature is reduced to 200-230 DEG C, has sulfocompound H in raw gas
2s and COS, and ammonia and prussiate impurity.Crude synthesis gas enters circulating fluidized bed dry thermally desulfurizing device 200.Sulfur-containing impurities in crude synthesis gas is by reacting with the active metal oxide MO in the sorbent material in the desulphurization reactor in circulating fluidized bed dry thermally desulfurizing device 200, and produce the sorbent material MS being loaded with sulphur, M is the metal be present in solid adsorbent.Such as Zn.
In high-temperature synthesis gas after desulfurization, sulphur content can be reduced to 0.1-5ppmv, and temperature is 170-300 DEG C, enters fine de-sulfur protection bed apparatus 300.
In the regeneration reactor of the sorbent material MS being loaded with sulphur in circulating fluidized bed dry thermally desulfurizing device 200 and O
2carry out chemical reaction, the sorbent material MS being loaded with sulphur is regenerated, reaction generates SO
2gas.Rich SO2 gas temperature is 200-550 DEG C, enters downstream and goes to produce sulfuric acid or sulphur.
High temperature desulfurizing synthetic gas is by after fine de-sulfur protection bed apparatus 300, and sulphur content is reduced to <0.1ppm.Synthetic gas after fine de-sulfur is divided into two strands, and a part of synthetic gas enters non-sulfur-resisting transformation device 400.In non-sulfur-resisting transformation device 400, desulfurized syngas generation transformationreation, the temperature of synthetic gas increases to 250-550 DEG C.After conversion synthetic gas mixes without the synthetic gas converted with another strand after fine de-sulfur after in non-sulfur-resisting transformation device 400, after reclaiming heat, temperature is down to 230-300 DEG C, enter adsorption bed together and take off NH3/HCN device 500, remove the NH3/HCN in conversion synthetic gas by ADSORPTION IN A FIXED BED agent.
Synthetic gas after imurity-removal divides two strands of methanation devices entering SNG gas product production equipment, and wherein most of synthetic gas enters the transportation flow fluidized bed reaction device 810a of methanation device.The synthetic gas of solid catalyst and charging enters bottom this transportation flow fluidized bed reaction device 810a, synthetic gas generation methanation reaction.Due to solid and the efficient gas-particle heat transfer efficiency of gas can be realized in transportation flow fluidized bed reaction device 810a, and gas and solid reaction time in transportation flow fluidized bed reaction device 810a shorter, the temperature in this transportation flow fluidized bed reaction device 810a is controlled uniformly.
Go out the gas-particle two-phase of transportation flow fluidized bed reaction device 810a through cyclonic separation, gas enters heat reclaim unit 840, solid is through gas-solid heat exchange device, and after producing high pressure steam cooling, the catalytic production of methane reaction of next circulation is carried out in the bottom again entering transportation flow fluidized bed reaction device 810a.
Through the methanation gas of heat recuperation, after mixing with other one of the conversion synthetic gas after imurity-removal, enter adiabatic methanation reactor 820.In adiabatic methanation reactor 820, proceed methanation reaction, the temperature of adiabatic methanation reactor 820 exit gas is at 350 DEG C-550 DEG C, and its temperature is regulated by the conversion synthetic gas tolerance of the imurity-removal entering adiabatic methanation reactor 820.
After adiabatic methanation reactor 820 methanation reaction, gas temperature after heat reclaim unit 850 is reduced to 240-280 DEG C, enters in isothermal methanation reactor 830.Continue methanation reaction occurs in isothermal methanation reactor 830, isothermal methanation reactor 830 Outlet Gas Temperature is at 250-300 DEG C, go out the gas of isothermal methanation reactor 830 after heat reclaim unit 860, temperature is reduced to 100-150 DEG C, and after cooling, temperature is down to 25-40 DEG C.
Methane-rich gas after cooling enters PSA decarbonation device 600a, at methane-rich gas in this device after the drying that dewaters, enters PSA pressure swing adsorber and removes CO in gas
2, finally obtain qualified SNG product.
Embodiment 4
Be with the difference being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of embodiment 2 see the circulating fluidized bed dry desulfurization production synthetic natural gas system that is combined shown in Fig. 4, figure:
Adsorption bed takes off NH
3/ HCN device 500 also has a removing impurities conversion syngas outlet 530 and increases by a device for producing hydrogen, and this device for producing hydrogen comprises the non-sulfur-resisting transformation device 1100 of low temperature, heat reclaim unit 1200, refrigerating unit 1300, PSA refining plant 1400.
The removing impurities conversion synthetic gas entrance 1110 of the non-sulfur-resisting transformation device 1100 of low temperature takes off NH by pipeline 17 and adsorption bed
3removing impurities conversion syngas outlet 530 in/HCN device 500 connects.
The low temperature shift synthetic gas entrance 1210 of heat reclaim unit 1200 is connected by the low temperature shift syngas outlet 1120 of the non-sulfur-resisting transformation device 1100 of pipeline 18 and low temperature.
The low temperature shift synthetic gas entrance 1310 of refrigerating unit 1300 is connected with the low temperature shift syngas outlet 1220 of heat reclaim unit 1200 by pipeline 19.
The low temperature shift syngas outlet 1320 of refrigerating unit 1300 is connected with the low temperature shift synthetic gas entrance 1410 of PSA refining plant 1400 by pipeline 20, and the hydrogen outlet 1420 of PSA refining plant 1400 sends qualified hydrogen.
The working process being combined circulating fluidized bed dry desulfurization production synthetic natural gas system of this embodiment is as follows:
Coal water slurry produces crude synthesis gas through coal water slurry gasifying device 900 sulfocompound H
2s and COS, and the impurity such as ammonia and prussiate.Crude synthesis gas is after Quench washing device 100 washs, and temperature is 220-240 DEG C.This crude synthesis gas enters circulating fluidized bed dry thermally desulfurizing device 200.Sulfur-containing impurities in crude synthesis gas is by reacting with the active metal oxide MO in the sorbent material in the desulphurization reactor in circulating fluidized bed dry thermally desulfurizing device 200, and produce the sorbent material MS being loaded with sulphur, M is the metal be present in solid adsorbent.Such as Zn.
In high-temperature synthesis gas after desulfurization, sulphur content can be reduced to 0.1-5ppmv, and temperature is 170-300 DEG C, enters fine de-sulfur protection bed apparatus 300.
In the regeneration reactor of the sorbent material MS being loaded with sulphur in circulating fluidized bed dry thermally desulfurizing device 200 and O
2carry out chemical reaction, the sorbent material MS being loaded with sulphur is regenerated, reaction generates SO
2.Rich SO
2gas temperature is 200-550 DEG C, enters downstream and goes to produce sulfuric acid or sulphur.
High temperature desulfurizing synthetic gas is by after fine de-sulfur protection bed apparatus 300, and sulphur content is reduced to <0.1ppm.
Synthetic gas after fine de-sulfur is divided into two strands, and a part of synthetic gas enters non-sulfur-resisting transformation device 400.In non-sulfur-resisting transformation device 400, desulfurized syngas generation transformationreation, the temperature of synthetic gas increases to 250-550 DEG C.After conversion synthetic gas mixes without the synthetic gas converted with another strand after fine de-sulfur after in non-sulfur-resisting transformation device 400, after reclaiming heat, temperature is down to 230-300 DEG C, enter adsorption bed together and take off NH3/HCN device 500, remove the NH3/HCN in conversion synthetic gas by ADSORPTION IN A FIXED BED agent.
Conversion synthetic gas after imurity-removal is divided into two portions, and the methanation device wherein in part feeding SNG gas product production equipment is for the production of synthetic natural gas, and a part sends into device for producing hydrogen for the production of hydrogen in addition.
The conversion synthetic gas sent into after the imurity-removal of the methanation device in SNG gas product production equipment is divided into two strands, major part wherein enters the adiabatic methanation reactor 810 of the methanation unit in SNG gas product production equipment, in adiabatic methanation reactor 810, most CO, part CO in synthetic gas
2and H
2reaction generates methane.Go out the synthetic gas temperature of adiabatic methanation reactor 810 at 540 DEG C-600 DEG C, its temperature is by the CO in the water vapor amount allocated into before non-sulfur-resisting transformation device 400, conversion synthetic gas
2concentration and control without the high-temperature fine desulfurized syngas flow of non-sulfur-resisting transformation device 400 and regulate.
After adiabatic methanation reactor 810 methanation reaction, gas temperature after heat reclaim unit 840 is reduced to 250-300 DEG C, enters adiabatic methanation reactor 820 after mixing with other one of the conversion synthetic gas after imurity-removal.Continue methanation reaction occurs in adiabatic methanation reactor 820, the Outlet Gas Temperature of adiabatic methanation reactor 820 is at 350 DEG C-550 DEG C, and its temperature is regulated by the conversion synthetic gas tolerance of the imurity-removal entering adiabatic methanation reactor 820.
After the reaction of adiabatic methanation reactor 820 methane alkane, gas temperature after heat reclaim unit 850 is reduced to 240-280 DEG C, enters isothermal methanation reactor 830.Continue methanation reaction occurs in isothermal methanation reactor 830, the Outlet Gas Temperature of isothermal methanation reactor 830 is at 250 DEG C-300 DEG C, after heat reclaim unit 860, methane rich synthetic gas temperature is reduced to 100-150 DEG C, and after refrigerating unit 870 cools, temperature is down to 30-75 DEG C.Methane rich synthetic gas after cooling enters MDEA decarbonation device 600, to remove the carbonic acid gas in synthetic gas, then enters TEG dehydration device 700 and removes water in synthetic gas, finally obtain SNG gas product.
Conversion synthetic gas part after imurity-removal enters device for producing hydrogen.Conversion synthetic gas is introduced into the non-sulfur-resisting transformation device 1100 of low temperature, continues transformationreation occurs, the CO in synthetic gas is all transformed into H in the non-sulfur-resisting transformation device 1100 of this low temperature
2and CO
2, the gas temperature going out the non-sulfur-resisting transformation device 1100 of low temperature is 200-280 DEG C, and the hydrogen-rich synthetic gas after conversion is reduced to 100-150 DEG C through heat reclaim unit 1200, and after refrigerating unit 1300 cools, temperature is down to 25-40 DEG C and is entered PSA refining plant 1400.
In PSA refining plant 1400, hydrogen-rich synthetic gas, after the drying that dewaters, enters PSA pressure swing adsorber and removes CO2 in gas, then enter PSA pressure-variable adsorption and carry hydrogen production device, finally obtain highly purified H2, send into downstream hydrogen subscriber unit, as synthetic ammonia installation or refinery's hydrogenation unit.
Claims (12)
1. be combined a system for circulating fluidized bed dry thermally desulfurizing production synthetic natural gas or coproduction hydrogen manufacturing, it is characterized in that, comprising:
Quench washing device, described Quench washing device has a crude synthesis gas input aperture and the first crude synthesis gas delivery port, and described crude synthesis gas input aperture is connected by pipeline with the crude synthesis gas delivery port of a crude synthesis gas forming apparatus;
The hot method desulfurizer of circulating fluidized bed, described circulating fluidized bed hot method desulfurizer has one first crude synthesis gas input aperture and high temperature desulfurizing syngas outlet and rich SO
2pneumatic outlet, described first crude synthesis gas input aperture is connected by pipeline with the first crude synthesis gas delivery port of described Quench washing device; Described rich SO
2pneumatic outlet sends rich SO
2gas is to sulfuric acid production plant or sulphur production installation;
Fine de-sulfur protection bed apparatus, described fine de-sulfur protection bed apparatus has high temperature desulfurizing synthetic gas entrance and the outlet of high-temperature fine desulfurized syngas, and described high temperature desulfurizing synthetic gas entrance is connected by the high temperature desulfurizing syngas outlet of the hot method desulfurizer of pipeline and described circulating fluidized bed;
Non-sulfur-resisting transformation device, described non-sulfur-resisting transformation device has high-temperature fine desulfurized syngas entrance and conversion syngas outlet, and described high-temperature fine desulfurized syngas entrance is protected the high-temperature fine desulfurized syngas of bed apparatus to export by pipeline and described fine de-sulfur to be connected;
Adsorption bed takes off NH
3/ HCN device, described adsorption bed takes off NH
3/ HCN device has conversion synthetic gas entrance and at least one removing impurities conversion syngas outlet, and described conversion synthetic gas entrance is connected by the conversion syngas outlet of pipeline with described non-sulfur-resisting transformation device;
SNG gas product production equipment, described SNG gas product production equipment has removing impurities conversion synthetic gas entrance and SNG product gas outlet, and the removing impurities conversion synthetic gas entrance of described SNG gas product production equipment takes off NH by pipeline and described adsorption bed
3the removing impurities conversion syngas outlet of/HCN device connects, and described SNG product gas outlet sends SNG gas product.
2. the system as claimed in claim 1, is characterized in that, described adsorption bed takes off NH
3the conversion synthetic gas entrance of/HCN device is also protected the high-temperature fine desulfurized syngas in bed apparatus to export by a high-temperature fine desulfurized syngas line of pipes with described fine de-sulfur to be connected.
3. system as claimed in claim 2, it is characterized in that, described adsorption bed takes off NH
3/ HCN device has two removing impurities conversion syngas outlet, be divided into the first removing impurities conversion syngas outlet and the second removing impurities conversion syngas outlet, wherein the first removing impurities conversion syngas outlet is converted synthetic gas entrance with the described removing impurities in described SNG gas product production equipment and is connected by pipeline; Describedly realize the above-mentioned system being combined the method for circulating fluidized bed dry desulfurization production synthetic natural gas or coproduction hydrogen manufacturing and also comprise a device for producing hydrogen, described device for producing hydrogen also has removing impurities conversion synthetic gas entrance and hydrogen outlet, and the removing impurities conversion synthetic gas entrance of described device for producing hydrogen takes off NH by pipeline and described adsorption bed
3second removing impurities conversion syngas outlet of/HCN device connects.
4. system as claimed in claim 3, is characterized in that, the pipeline between the outlet of high-temperature fine desulfurized syngas and the high-temperature fine desulfurized syngas entrance of described non-sulfur-resisting transformation device of described fine de-sulfur protection bed apparatus is also connected with a water vapour and supplements and manage.
5. system as claimed in claim 5, it is characterized in that, described SNG gas product production equipment comprises:
First methanation reaction device, described first methanation reaction device has removing impurities conversion synthetic gas entrance and the outlet of the first methanation reaction gas, and the removing impurities conversion synthetic gas entrance of described first methanation reaction device takes off NH by pipeline and described adsorption bed
3removing impurities conversion syngas outlet in/HCN device or the first removing impurities conversion syngas outlet connect;
Second heat reclaim unit, described second heat reclaim unit has the first methanation reaction gas entrance and the outlet of the second methanation reaction gas, and described first methanation reaction gas entrance is exported with the first methanation reaction gas of described first methanation reaction device and is connected by pipeline;
Second methanation reaction device, described second methanation reaction device has the second methanation reaction gas entrance and the outlet of front three alkanisation reaction gas, described second methanation reaction gas entrance to be exported with the second methanation reaction gas of described second heat reclaim unit by pipeline and is connected, and described second methanation reaction gas entrance also takes off NH by a removing impurities conversion synthetic gas line of pipes and described adsorption bed
3removing impurities conversion syngas outlet in/HCN device or the first removing impurities conversion syngas outlet connect;
3rd heat reclaim unit, described 3rd heat reclaim unit has front three alkanisation reaction gas entrance and the outlet of the 4th methanation reaction gas, and described front three alkanisation reaction gas entrance is exported with the front three alkanisation reaction gas of described second methanation reaction device and is connected by pipeline;
Front three alkanisation reaction unit, described front three alkanisation reaction unit has the 4th methanation reaction gas entrance and the outlet of the 5th methanation reaction gas, and described 4th methane reaction gas entrance to be exported with the 4th methanation reaction gas of described 3rd heat reclaim unit by pipeline and is connected;
4th heat reclaim unit, described 4th heat reclaim unit has the 5th methanation reaction gas entrance and the first methane rich syngas outlet, and described 5th methanation reaction gas entrance to be exported with the 5th methanation reaction gas of described front three alkanisation reaction unit by pipeline and is connected;
Second refrigerating unit, described second refrigerating unit has the first methane rich synthetic gas entrance and the second methane rich syngas outlet, and described first methane rich synthetic gas entrance is connected with the first methane rich syngas outlet of described heat reclaim unit by pipeline;
CO2 removal device, described CO2 removal device has the second methane rich synthetic gas entrance and SNG product gas outlet, described second methane rich synthetic gas entrance is connected with the second methane rich syngas outlet of described second refrigerating unit by pipeline, and described SNG product gas outlet sends SNG gas product.
6. system as claimed in claim 5, it is characterized in that, also comprise a drying and dehydrating device, described drying installation has SNG gas product entrance and dried SNG product gas outlet, and the SNG gas product entrance of described drying and dehydrating device is connected with the SNG product gas outlet in described CO2 removal device by pipeline; The dried SNG product gas outlet of described drying and dehydrating device sends dried SNG gas product.
7. system as claimed in claim 6, is characterized in that, described first methanation reaction device is conveying bed methanation reaction device or adiabatic methanation reaction unit.
8. system as claimed in claim 7, it is characterized in that, described second methanation reaction device is adiabatic methanation reaction unit.
9. system as claimed in claim 8, it is characterized in that, described front three alkanisation reaction unit is isothermal methanation reaction unit.
10. system as claimed in claim 9, it is characterized in that, described device for producing hydrogen comprises:
The non-sulfur-resisting transformation device of low temperature, the non-sulfur-resisting transformation device of described low temperature has removing impurities conversion synthetic gas entrance and the first low temperature shift syngas outlet, and the removing impurities conversion synthetic gas entrance of described low temperature non-sulfur-resisting transformation device takes off NH by pipeline and described adsorption bed
3the second removing impurities conversion syngas outlet in/HCN device connects;
First heat reclaim unit, described first heat reclaim unit has the first low temperature shift synthetic gas entrance and the second low temperature shift syngas outlet, and described first low temperature shift synthetic gas entrance is connected by pipeline with the first low temperature shift syngas outlet of the non-sulfur-resisting transformation device of described low temperature;
First refrigerating unit, described first refrigerating unit has the second low temperature shift synthetic gas entrance and the 3rd low temperature shift syngas outlet, and described second low temperature shift synthetic gas entrance is connected by pipeline with the second low temperature shift syngas outlet of described first heat reclaim unit;
Refining plant, described refining plant has the 3rd low temperature shift synthetic gas entrance and hydrogen outlet, and described 3rd low temperature shift synthetic gas entrance is connected by pipeline with the 3rd low temperature shift syngas outlet of described first refrigerating unit; Described hydrogen outlet sends qualified hydrogen.
11. systems as claimed in claim 10, it is characterized in that, described refining plant is PSA refining plant.
12. systems as claimed in claim 11, it is characterized in that, described crude synthesis gas forming apparatus is coal water slurry gasifying device or gasifying powder coal device.
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