CN102320568A - Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation - Google Patents
Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation Download PDFInfo
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Abstract
The invention discloses a method and a device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation. The method comprises the following steps: directly sending crude gas at an outlet of a BGL furnace into a pure oxygen non-catalytic partial oxidation furnace and combusting with the preheated pure oxygen, forming high temperature gas and then sending to prepare qualified synthetic gas or hydrogen. According to the invention, the high temperature combustion of partial oxidation furnace is conversed to useful ingredients or simple substances which are easy to be removed and processed. Such as methane and light oil are conversed to useful medium hydrogen and carbon monoxide; thiophene is conversed to hydrogen sulfide and the like. The invention also discloses a device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation.
Description
Technical field
The present invention relates to the coal is that raw material is produced synthetic gas or the hydrogen of hydrogen and the carbon monoxide technical field with system synthetic oil, synthetic ammonia or methyl alcohol etc., and particularly the gasification of BGL pressurization slag adds method and the device that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen.
Background technology
At present be with the coal raw material Coal Gasification Technology comparative maturity of producing hydrogen and carbon monoxide synthetic gas or hydrogen have following several kinds:
1.SHELL/GSP dry coal powder gasification is technological.It is high that this technology introduction software takes, and coal required high, and operational condition is harsh, vapourizing furnace device structure complicated (stove internals particularly, at present domestic still do not possess processing and manufacturing ability completely), and facility investment is big.All there are not sophisticated device and experience to use for reference both at home and abroad.Because investment is high, the start-stop car often, product cost is high, even domestic SHELL/GSP device of having driven also is earnestly to support, some has been gone bankrupt by also.Country has suspended the construction of newly-built SHELL gasification installation.
2. coal water slurry gasification is technological.This technology requires high to coal, operational condition is harsh, and the maintenance of pure oxygen burner is frequent, and pulping process is complicated, and investment is big, limited by coal adaptability.
3.LURGI the stove crushed coal pressure gasifying is technological.Technology maturation, vapourizing furnace equipment is simple, can domesticize; Operational condition is gentle, and the oxygen consumption is low, and facility investment is low; Adapt to low grade coal; But the gas liquor treatment scheme is long, complex process; Raw gas purifying and methane component reclaim and utilize technical process long and complicated, and investment is big, and energy consumption is high.
4.BGL pressurization slag gasification technology.This technical matters principle and LURGI stove crushed coal pressure gasifying technology are basic identical, but its shortcoming has been carried out significantly improving: for example significantly reduce process steam consumption, reduce the scale of steam boiler; Significantly reduce efflux the coal gas water yield (for lurgi gasifier crushed coal pressure gasifying technology 10～15%), reduce the scale of gas liquor processing/WWT; Significantly reduce carbon residue content in the gasification ashes (assurance is lower than 0.5%, and lurgi gasifier is about 5%, controls to be lower than 6%); Separate unit vapourizing furnace production intensity significantly promotes (be lurgi gasifier 1.5～2 times).But the shortcoming that it does not have thoroughly to eliminate lurgi gasifier in essence for example contains methane in the synthetic gas, contains complicated organic impurity etc. in the gas liquor.
5. atmosphere intermission air coal (Jiao) gas making bed technology.This technology throughput is low, seriously polluted, and energy consumption is high.The domestic project begun newly of forbidding already adopts.
6. continuous oxygen enrichment of normal pressure or pure oxygen coal (Jiao) gas making bed technology.This technology throughput is low, seriously polluted, and energy consumption is high.Domestic project begun newly seldom adopts.
Adopt BGL stove coal generating gas to produce the technological process of hydrogen and carbon monoxide synthetic gas or hydrogen, some problems below existing:
1. the more and complicated component of organic content in the raw gas washing water (gas liquor) recycles difficulty, and investment is big.
2. contain a large amount of methane pact～8%V in the raw gas and do, reclaim and utilize difficulty, the long flow path investment is big; As do not reclaim then and waste raw material; Methane gets into the efficient that the subsequent technique device will reduce follow up device such as for example coal system is oily, methyl alcohol is synthetic, and the amount of discharging increases the available gas utilization ratio and reduces.
3. contain in the raw gas impurity such as the organosulfur of raw gas purifying device such as low-temperature rectisol or transformation adsorbing and removing difficulty such as thiophene, carbon oxysulfide, disulfides other than hydrogen; Also contain the organism that pollutes low temperature washing device for methanol such as tar, middle oil, light oil constituents; Handle and reclaim difficulty, investment is big.
4.BGL the high temperature rough gas of outlet of still can only the by-product LP steam, the steam grade is low, and energy utilization efficiency is low.
Summary of the invention
One of technical problem to be solved by this invention is to produce the existing problem of technological process of hydrogen and carbon monoxide synthetic gas or hydrogen and provide the gasification of a kind of BGL pressurization slag to add the method that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen to BGL stove coal generating gas; This method can make BGL stove coal generating gas produce hydrogen and carbon monoxide synthetic gas or hydrogen, and to be used for the process more economical of device such as coal system oil, synthetic ammonia, methyl alcohol reasonable; Give full play to the advantage that BGL stove coal generating gas investment is low, consume low, technology maturation and production domesticization, thoroughly solve the problem that present BGL stove coal generating gas technology exists.
Two of technical problem to be solved by this invention is to provide the gasification of a kind of above-mentioned BGL pressurization slag to add the employed device of method that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen.
BGL pressurization slag gasification as first aspect present invention adds the method that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen; Its BGL outlet of still raw gas is directly sent into the pure oxygen non-catalytic partial oxidation stove; Burn with pure oxygen through preheating; 170 ℃ of left and right sides gases of final formation are seen off, further produce qualified synthetic gas or hydrogen.
In a preferred embodiment of the inventive method; The high-temperature gas that said pure oxygen non-catalytic partial oxidation stove is seen off is after the heat recuperation step reclaims the heat and the second dust removal step dedusting; Sending into the desulfurization and decarburization step carries out forming the purification synthetic gas behind the desulfurization and decarburization; This purification synthetic gas is sent into essence and is taken off purification step and further purify, and forms qualified synthetic gas or hydrogen and sees off.
In a preferred embodiment of the inventive method, said BGL outlet of still raw gas is directly sent into the pure oxygen non-catalytic partial oxidation stove after the first dust removal step dedusting.
In a preferred embodiment of the inventive method; The high-temperature gas of said pure oxygen non-catalytic partial oxidation stove is sent into sulfur-resisting transformation step adjustment hydrogen/carbon monoxide ratio and is about 1: 1～3: 1 after the heat recuperation step reclaims the heat and the second dust removal step dedusting; Conversion coal gas after adjustment hydrogen/carbon monoxide ratio is sent into the desulfurization and decarburization step and is carried out desulfurization and decarburization.
In a preferred embodiment of the inventive method, through the raw gas after the second dust removal step dedusting or after the raw gas of adjustment after hydrogen/carbon monoxide ratio is cooled to through a cooling step, send into the desulfurization and decarburization step and carry out desulfurization and decarburization.
In a preferred embodiment of the inventive method; The pure oxygen that gets into the pure oxygen non-catalytic partial oxidation stove is from the sky branch; Mass percent concentration is 90～99.6%; Temperature is normal temperature～150 ℃, and the temperature of BGL outlet of still raw gas is 350～650 ℃, and the volume ratio of pure oxygen and BGL outlet of still raw gas is 0.1～0.2.
In a preferred embodiment of the inventive method, but by-product 4.0～10.OMPa mesohigh saturation steam and/or 0.5～0.6MPa low-pressure saturated steam in the said heat recuperation step, and the gas liquor of formation goes gas liquor to separate and treatment system.
In a preferred embodiment of the inventive method, the raw gas temperature that said heat recuperation step is seen off is about 140～150 ℃.
In a preferred embodiment of the invention, said sulfur-resisting transformation step part conversion or all conversion raw gas.
In a preferred embodiment of the inventive method; Said desulfurization and decarburization step is low-temperature rectisol step or transformation adsorption step, and wherein the low-temp methanol regeneration of coming out is rich in hydrogen sulfide or transformation adsorption step tail gas discharged and is sent into the sulfur recovery step and produce sulphur or sulfuric acid as producing sulphur or vitriolic virgin gas.
In a preferred embodiment of the inventive method, said first dust removal step adopts high temperature cyclone separator to carry out.
In a preferred embodiment of the inventive method, said heat recuperation step adopts cold shock and/or waste heat boiler to carry out.
In a preferred embodiment of the inventive method, said second dust removal step is divided into washing step and cyclonic separation step, and the gas liquor that said cyclonic separation step forms goes gas liquor to separate and treatment system.
Hydrogen/carbon monoxide the ratio of said qualified synthetic gas is 1～3: 1 or the hydrogen rich gas product.
BGL pressurization slag gasification as second aspect present invention adds the device that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen; Comprise BGL vapourizing furnace and pure oxygen non-catalytic partial oxidation stove; Wherein the outlet of the raw gas on the BGL vapourizing furnace is connected on the raw gas inlet of pure oxygen non-catalytic partial oxidation stove through the first raw gas transfer lime, and the pure oxygen inlet on the said pure oxygen non-catalytic partial oxidation stove connects the pure oxygen delivery port of air separation plant through the pure oxygen input tube; The raw gas that high-temperature gas outlet on the pure oxygen non-catalytic partial oxidation stove is seen off is to produce qualified synthetic gas or hydrogen.
In a preferred embodiment of apparatus of the present invention; Also comprise one first tripping device; Said first tripping device is provided with raw gas inlet, raw gas outlet, the outlet of powder ash; Raw gas inlet on first tripping device connects the first raw gas transfer lime, and the raw gas outlet of first tripping device enters the mouth through the raw gas that the second raw gas transfer lime connects said pure oxygen non-catalytic partial oxidation stove, and dust is seen in the powder ash outlet of first tripping device off.
In a preferred embodiment of apparatus of the present invention, first tripping device is a Cyclonic separating apparatus.
In a preferred embodiment of apparatus of the present invention; Also comprise a thermal recovery unit; Said thermal recovery unit is provided with high-temperature gas inlet, high-temperature gas outlet, vapour outlet and gas liquor outlet; The high-temperature gas inlet of said thermal recovery unit connects the high-temperature gas outlet on the said pure oxygen non-catalytic partial oxidation stove through the high-temperature gas transfer lime; During seeing off, the vapour outlet of this thermal recovery unit presses and/or low-pressure saturated steam; The gas liquor outlet of thermal recovery unit connects gas liquor through the first gas liquor transfer lime and separates and treatment system, and the raw gas that the high-temperature gas outlet on the thermal recovery unit is seen off is to produce qualified synthetic gas or hydrogen.
In a preferred embodiment of apparatus of the present invention; Also be provided with gas liquor inlet on the said pure oxygen non-catalytic partial oxidation stove, the gas liquor inlet on the said pure oxygen non-catalytic partial oxidation stove connects gas liquor through the second gas liquor transfer lime to be separated and treatment system.
In a preferred embodiment of apparatus of the present invention, the said first gas liquor transfer lime is connected the second gas liquor transfer lime through first connection line with compressor.
In a preferred embodiment of apparatus of the present invention; Also comprise one second tripping device; Said second tripping device is provided with gas inlet and pneumatic outlet and gas liquor outlet; Gas inlet on said second tripping device connects the high-temperature gas outlet on the said thermal recovery unit through the 3rd raw gas transfer lime; The raw gas that pneumatic outlet on second tripping device is seen off, to produce qualified synthetic gas or hydrogen, the gas liquor outlet on second tripping device is connected with the said first gas liquor transfer lime.
In a preferred embodiment of apparatus of the present invention, said second tripping device is the washing Cyclonic separating apparatus.
In a preferred embodiment of apparatus of the present invention; Also comprise a refrigerating unit; Said refrigerating unit is provided with raw gas inlet, raw gas outlet and gas liquor outlet; Raw gas on said refrigerating unit inlet is connected with pneumatic outlet on said second tripping device through pipeline; The raw gas that raw gas outlet on the refrigerating unit is seen off, to produce qualified synthetic gas or hydrogen, the gas liquor outlet on the refrigerating unit connects gas liquor through the 3rd gas liquor transfer lime and separates and treatment system.
In a preferred embodiment of apparatus of the present invention; Between said refrigerating unit and said second tripping device, increase by a sulfur-resisting transformation device; Said sulfur-resisting transformation device comprises a heat-exchange equipment and a conversion equipment; Said heat-exchange equipment is provided with raw gas inlet, raw gas outlet, the outlet of conversion gas, conversion gas loop head, and said conversion equipment is provided with raw gas inlet, conversion gas loop exit; Pneumatic outlet on said second tripping device connects the raw gas inlet on the said heat-exchange equipment through the 4th raw gas transfer lime on the one hand, connects the raw gas inlet on the said refrigerating unit through the 5th raw gas transfer lime and valve on the other hand; Conversion gas outlet on the said heat-exchange equipment connects the raw gas inlet on the said refrigerating unit through the conversion letter shoot; Raw gas outlet on the heat-exchange equipment connects the raw gas inlet on the said conversion equipment through the 6th raw gas transfer lime, and the conversion gas loop exit on the conversion equipment connects the conversion gas loop head on the heat-exchange equipment through conversion gas circulation tube.
In a preferred embodiment of apparatus of the present invention; Also comprise a desulfurization and decarburization device; Said desulfurization and decarburization device is provided with raw gas inlet, clean gas outlet and production sulphur or the outlet of vitriolic virgin gas; Raw gas inlet on the said desulfurization and decarburization device connects the raw gas outlet on the refrigerating unit through the 7th raw gas transfer lime, and the purified gas that the clean gas outlet on the desulfurization and decarburization device is seen off is to produce qualified synthetic gas or hydrogen; Virgin gas outlet on the said desulfurization and decarburization device is seen off and is produced sulphur or vitriolic virgin gas.
In a preferred embodiment of apparatus of the present invention, said desulfurization and decarburization device is low-temperature rectisol equipment or variable-pressure adsorption equipment.
In a preferred embodiment of apparatus of the present invention; Also comprise a sulfur recovery unit; Said sulfur recovery unit is provided with virgin gas inlet and sulphur or sulfuric acid outlet; Virgin gas inlet on the sulfur recovery unit connects the virgin gas outlet on the said desulfurization and decarburization device through the virgin gas transfer lime, and sulphur or sulfuric acid are seen in sulphur on the sulfur recovery unit or sulfuric acid outlet off.
In a preferred embodiment of apparatus of the present invention; Comprise that also an essence takes off equipment; Said essence is taken off equipment and is provided with purified gas inlet, syngas outlet; The purified gas inlet that essence is taken off on the equipment connects the clean gas outlet on the desulfurization and decarburization device through the purified gas transfer lime, and the syngas outlet that essence is taken off on the equipment is carried qualified synthetic gas or hydrogen.
Owing to adopted technical scheme as above, the present invention compared with prior art has following advantage:
1.BGL the outlet of still raw gas can adopt high temperature cyclone separator to remove most of dry dust, reduces the erosion corrosion influence of high-temperature dust to follow-up equipment, reduces dust content in the gas liquor, it is mobile to improve gas liquor.
2. the raw gas after high temperature cyclone dust removal directly gets into pure oxygen non-catalytic partial oxidation stove (POX) and burns through the pure oxygen of preheating, produces high temperature, fully the organism in the cracking conversion raw gas.
3. the high-temperature gas that goes out partial oxidation furnace (POX) can be taked to press and/or low-pressure saturated steam recovery heat in cold shock and/or the useless pot by-product.
4. the raw gas after heat recuperation further removes the dust of deentrainment again through washing and cyclonic separation.
5. raw gas can be adjusted final hydrogen/carbon monoxide ratio through sulfur-resisting transformation, satisfies the subsequent technique requirement.
6. raw gas adopts low-temperature rectisol or transformation absorption or additive method refining plant desulfurization and decarburization.
7. take off refining plant through the synthetic gas employing essence of refining plant synthetic gas is further purified, guarantee synthetic gas or hydrogen quality.
Crushed coal pressure gasifying technology and coal water slurry gasification technology are that use is the most extensive at present, two kinds of Coal Gasification Technology that vaporization ability is maximum.BGL pressurization slag gasification technology technological principle and crushed coal pressure gasifying technology type have seemingly still improved the efficient of gasification greatly.BGL pressurization slag gasification deslagging principle and coal water slurry gasification technology type are seemingly; Non-catalytic partial oxidation principle of the present invention also with the coal water slurry gasification technology type seemingly; But because BGL pressurization slag gasification+POX adopts superheated vapour to advance vapourizing furnace; Be different from the liquid coal slurry charging of coal water slurry gasification technology, can expect that therefore BGL pressurization slag gasification+POX will obtain the oxygen consumption lower than the coal water slurry gasification technology, and obtain similar gas liquor and can adopt low grade coal as raw material.
After adopting the present invention; Synthetic gas or the hydrogen of producing hydrogen and carbon monoxide with BGL stove coal generating gas is used for the technical process and the auxiliary facility of processes such as coal system oil, methyl alcohol are synthetic, ammonia synthesis to be simplified greatly, advantage comprise gas liquor separate simplify, phenol ammonia reclaims cancellation and WWT simplification, raw gas purifying reliable and stable, methane recovery and handle workshop section's cancellation or the like; Another benefit is the requirement that partial oxidation furnace (POX) outlet proportion of composing satisfies follow-up coal system wet goods technological process basically, can not adopt the part sulfur-resisting transformation to put forward the method that hydrogen is regulated hydrogen/carbon monoxide ratio once more through decarburization.
The organic impurity that contains the subsequent technique dealing with complicated in the raw gas of BGL stove production adopts the high-temp combustion of partial oxidation furnace of the present invention (POX), all is converted into useful component or is easy to remove easy-to-handle simple material.For example methane and light oil are converted into useful medium hydrogen and carbon monoxide; Thiophene is converted into hydrogen sulfide etc.
The present invention has following clear superiority:
1. do not contain impurity such as naphthalene, thiophene and higher hydrocarbon in the raw gas; Low-temperature rectisol or pressure swing adsorption purge device are reliable stable; Do not cause the problem that impurity accumulation operation worsens in the methanol solution thereby do not exist, do not have the problem of polluting transformation absorption sorbent material because pollute methanol solution.
2. cancellation and supporting necessary methane recovery of former BGL stove coal generating gas and processing workshop section, for example low temperature separation process methane workshop section (like liquid nitrogen washing) and methane conversion recycle section shorten flow process greatly, simplify the operation, practice thrift investment, cut down the consumption of energy.
Description of drawings
Fig. 1 is the skeleton diagram of apparatus of the present invention.
Embodiment
In order to make technique means of the present invention, creation characteristic, to reach purpose and effect and be easy to understand and understand,, further set forth the present invention below in conjunction with specific embodiment.
Following examples are with certain coal synthesis ammonia device, and the synthetic gas that adopts BGL stove coal generating gas to produce hydrogen or carbon monoxide is that example is explained the present invention.
Referring to Fig. 1; The gasification of the BGL of present embodiment pressurization slag adds the device that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas, comprises that BGL vapourizing furnace 10, high temperature cyclone separator 20, pure oxygen non-catalytic partial oxidation stove 30, waste heat boiler 40, washing cyclonic separator 50, sulfur-resisting transformation equipment 60, cooling apparatus 70, low-temperature rectisol equipment 80, sulfur recovery unit 90, essence take off equipment 100.Wherein waste heat boiler 40 can use replacement of cold shock equipment or waste heat boiler 40 to replace with cold shock equipment mixing use, and low-temperature rectisol equipment 80 can use variable-pressure adsorption equipment to replace.
BGL stove coal Gasification Technology in Retrospect adopts BGL pressurization slag gas-making process, is raw material with the broken coal, and pure oxygen and steam are oxygenant/vaporized chemical, static bed gas making, slag tap.Broken coal, steam and pure oxygen are got in the BGL stove vapourizing furnace 10 by coal inlet 11, steam-in 12, the pure oxygen inlet 13 of BGL stove vapourizing furnace 10 respectively, and lime-ash is discharged by the slag-drip opening 14 of BGL stove vapourizing furnace 10.Pure oxygen is carried through pure oxygen transfer lime 111 by air separation plant 110 and is come.
The ratio of hydrogen/carbon monoxide is about 0.72 in the about 400 ℃ raw gas that is come out by the raw gas of BGL stove vapourizing furnace 10 outlet 15, and contains the methane of 7.4%V.
The raw gas condition is following: %V does
Other impurity are following:
Dust, tar, middle oil, light oil, phenol, lipid acid, ammonia, prussiate.
The about 400 ℃ raw gas that is come out by the raw gas of BGL stove vapourizing furnace 10 outlet 15 enters the mouth through raw gas transfer lime 15 and raw gas on the high temperature cyclone separator 20 and 21 sends into high temperature cyclone separator 20 and separate; The raw gas of removing most of dust is directly sent in the pure oxygen non-catalytic partial oxidation stove 30 through the raw gas inlet 31 of the outlet 21 of the raw gas on the high temperature cyclone separator 20 and raw gas transfer lime 22, pure oxygen non-catalytic partial oxidation stove 30, and isolating dust is discharged through the ash of the powder on the high temperature cyclone separator 20 outlet 23.
Does the pure oxygen of air separation plant 110 add safe steam preheating extremely? Pure oxygen inlet 32 through pure oxygen transfer lime 112, pure oxygen non-catalytic partial oxidation stove 30 after ℃ is sent in the pure oxygen non-catalytic partial oxidation stove 30; With the raw gas of sending into mixed firing in pure oxygen non-catalytic partial oxidation stove 30; Produce high temperature, at this moment the organism in the raw gas comprises organosulfur such as thiophene etc. and cracking at high temperature, hydrogenation and conversions such as organic hydrocarbon such as methane.
Adopt pure oxygen non-catalytic partial oxidation stove 30 of the present invention (POX), hydrogen/carbon monoxide ratio is 0.55 in 170 ℃ of high-temperature gases that high-temperature gas outlet 33 is come out, and wherein methane content is less than 0.2%V.All impurity almost all are converted into the simplest CO
2, CO, H
2And water.
170 ℃ of high-temperature gases that come out by the high-temperature gas of pure oxygen non-catalytic partial oxidation stove 30 outlet 33 send into through the inlet of the high-temperature gas on high-temperature gas transfer lime 34, the waste heat boiler 40 41 that byproduct steams carry out heat recuperation in the waste heat boiler 40.Gas liquor inlet 35 on the pure oxygen non-catalytic partial oxidation stove 30 connects gas liquor through gas liquor transfer lime 36 to be separated and treatment system, in needs, to replenish gas liquor to pure oxygen non-catalytic partial oxidation stove 30.The concentration of volume percent that gets into pure oxygen non-catalytic partial oxidation stove 30 is 95%, and temperature is normal temperature～150 ℃, and the volume ratio of pure oxygen and BGL outlet of still raw gas is 0.1～0.2.
Waste heat boiler 40 is in reclaiming heat byproduct steam process; Raw gas through the heat recuperation temperature reduces is seen off by the outlet of the high-temperature gas on the waste heat boiler 40 42; By-product? Press among the MPa saturation steam and/or? The MPa low-pressure saturated steam is seen off by the vapour outlet on the waste heat boiler 40 43; The gas liquor that waste heat boiler 40 forms is seen off by the outlet of the gas liquor on it 44, and delivers to through gas liquor transfer lime 45 that gas liquor separates and treatment system is handled.Also be connected with compressor 47 between the gas liquor transfer lime 45 and 36 through connection line 46.
Be reduced to 140 ℃ raw gas through the heat recuperation temperature and sent in the washing cyclonic separator 50 through the gas inlet on raw gas transfer lime 48, the washing cyclonic separator 50 and wash and cyclonic separation by what the high-temperature gas on the waste heat boiler 40 outlet 42 was seen off, the gas liquor after the separation delivers to via gas liquor transfer lime 45 through the outlet 51 of the gas liquor on it that gas liquor separates and treatment system is handled.Pneumatic outlet 5 on the washing cyclonic separator 50 meets the raw gas inlet 61a on the interchanger 61 in the sulfur-resisting transformation device 60 through raw gas transfer lime 54 on the one hand, connects the raw gas inlet 71 on the refrigerating unit 70 through raw gas transfer lime 55 and valve 56 on the other hand.Can require to carry out part variation or whole conversion raw gas according to subsequent technique through valve 56 like this, be 1～3: 1 to regulate hydrogen/carbon monoxide ratio, produces synthetic gas or hydrogen.And after advancing heat exchange by the raw gas that interchanger 61 was brought and got into to raw gas transfer lime 54; Send into through the inlet of the raw gas on raw gas transfer lime 61d, the conversion equipment 62 62a by the raw gas on the interchanger 61 outlet 61c and to carry out conversion in the conversion equipment 61; After conversion gas after conversion equipment 62 conversion is come out by the conversion gas loop exit 62b on it; Get into interchanger 61 through the conversion gas loop head on conversion gas circulation tube 62c, the interchanger 61 and carry out heat exchange; Conversion gas through overregulating hydrogen/carbon monoxide ratio is come out by the outlet of the conversion gas on the interchanger 61 61b; Deliver in the refrigerating unit 70 through the inlet of the raw gas on conversion letter shoot 61c, the refrigerating unit 70 71 again and cool off, remove process condensate.
The gas liquor (process condensate) that refrigerating unit 70 cooling backs form delivers to the gas liquor separation through outlet 72 of the gas liquor on it and gas liquor transfer lime 73 and treatment system is handled.The raw gas that refrigerating unit 70 cooling backs form is sent into low-temperature rectisol equipment 80 by the raw gas inlet on the outlet of the raw gas on it 73, raw gas transfer lime 74 and the low-temperature rectisol equipment 80 and is purified.
After the purification produced be used to produce sulphur or vitriolic virgin gas and send into through the virgin gas outlet 91 on the production sulphur on the low-temperature rectisol equipment 80 or vitriolic virgin gas outlet 81, virgin gas transfer lime 82, the sulfur recovery unit 90 and reclaim sulphur in the sulfur recovery unit 90; Process sulphur or sulfuric acid, sulphur of processing or sulfuric acid are seen off through sulphur on the sulfur recovery unit 90 or sulfuric acid outlet 92.Purified gas after the purification is come out by the clean gas outlet on the low-temperature rectisol equipment 80 83; Take off purified gas inlet 101 on the equipment 100 through purified gas transfer lime 84, essence and send into essence and take off equipment 100 and carry out essence and take off, remove detrimental impurity to satisfying for example ammonia synthesizer of subsequent technique requirement.Hydrogen after essence is taken off/carbon monoxide ratio is that the syngas outlet 102 that 1～3: 1 qualified synthetic gas is taken off on the equipment 100 by essence is seen off.
More than show and described ultimate principle of the present invention, principal character and advantage of the present invention.The technician of the industry should understand; The present invention is not restricted to the described embodiments; That describes in the foregoing description and the specification sheets just explains principle of the present invention; The present invention also has various changes and modifications under the prerequisite that does not break away from spirit and scope of the invention, and these variations and improvement all fall in the scope of the invention that requires protection.The present invention requires protection domain to be defined by appending claims and equivalent thereof.
Claims (28)
1.BGL the gasification of pressurization slag adds the method that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen; It is characterized in that; BGL outlet of still raw gas is directly sent into the pure oxygen non-catalytic partial oxidation stove; Burn with pure oxygen, finally form 170 ℃ of gases and see off, to produce qualified synthetic gas or hydrogen through preheating.
2. the method for claim 1; It is characterized in that; The high-temperature gas that said pure oxygen non-catalytic partial oxidation stove is seen off is after the heat recuperation step reclaims the heat and the second dust removal step dedusting; Send into the desulfurization and decarburization step and carry out forming behind the desulfurization and decarburization and purify synthetic gas, this purification synthetic gas is sent into essence and is taken off purification step and further purify, and forms qualified synthetic gas or hydrogen and sees off.
3. according to claim 1 or claim 2 method is characterized in that said BGL outlet of still raw gas is directly sent into the pure oxygen non-catalytic partial oxidation stove after the first dust removal step dedusting.
4. method as claimed in claim 2; It is characterized in that; The high-temperature gas of said pure oxygen non-catalytic partial oxidation stove is after the heat recuperation step reclaims the heat and the second dust removal step dedusting, and sending into sulfur-resisting transformation step adjustment hydrogen/carbon monoxide ratio is 1: 1～3: 1; Raw gas after adjustment hydrogen/carbon monoxide ratio is sent into the desulfurization and decarburization step and is carried out desulfurization and decarburization.
5. like claim 2 or 4 described methods, it is characterized in that, through the raw gas after the second dust removal step dedusting or after the raw gas of adjustment after hydrogen/carbon monoxide ratio is through cooling step cooling, send into the desulfurization and decarburization step and carry out desulfurization and decarburization.
6. the method for claim 1; It is characterized in that; The pure oxygen that gets into the pure oxygen non-catalytic partial oxidation stove is from the sky branch, and concentration of volume percent is 90～99.6%, and temperature is normal temperature～150 ℃; The temperature of BGL outlet of still raw gas is 350～650 ℃, and the volume ratio of pure oxygen and BGL outlet of still raw gas is 0.1～0.2: 1.
7. the method for claim 1 is characterized in that, presses saturation steam and/or 0.5～0.6MPa low-pressure saturated steam in the said heat recuperation step among by-product 4.0～10.OMPa, and the gas liquor of formation goes gas liquor to separate and treatment system.
8. the method for claim 1 is characterized in that, the raw gas temperature that said heat recuperation step is seen off is 140～150 ℃.
9. method as claimed in claim 4 is characterized in that, said sulfur-resisting transformation step part conversion or whole conversion raw gas.
10. method as claimed in claim 2; It is characterized in that; Said desulfurization and decarburization step is low-temperature rectisol step or transformation adsorption step, and wherein the low-temp methanol regeneration of coming out is rich in hydrogen sulfide or transformation adsorption step tail gas discharged and is sent into the sulfur recovery step and produce sulphur or sulfuric acid as producing sulphur or vitriolic virgin gas.
11. method as claimed in claim 3 is characterized in that, said first dust removal step adopts high temperature cyclone separator to carry out.
12. method as claimed in claim 2 is characterized in that, said heat recuperation step adopts cold shock and/or waste heat boiler to carry out.
13. method as claimed in claim 2 is characterized in that, said second dust removal step is divided into washing step and cyclonic separation step, and the gas liquor that said cyclonic separation step forms goes gas liquor to separate and treatment system.
14. the method for claim 1 is characterized in that, the hydrogen/carbon monoxide ratio of said qualified synthetic gas is 1～3: 1 or the hydrogen rich gas product.
15. the described BGL pressurization of claim 1 slag gasification adds the employed device of method that pure oxygen non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen; It is characterized in that; Comprise BGL vapourizing furnace and pure oxygen non-catalytic partial oxidation stove; Wherein the outlet of the raw gas on the BGL vapourizing furnace is connected on the raw gas inlet of pure oxygen non-catalytic partial oxidation stove through the first raw gas transfer lime, and the pure oxygen inlet on the said pure oxygen non-catalytic partial oxidation stove connects the pure oxygen delivery port of air separation plant through the pure oxygen input tube; The raw gas that high-temperature gas outlet on the pure oxygen non-catalytic partial oxidation stove is seen off is to produce qualified synthetic gas or hydrogen.
16. device as claimed in claim 16; It is characterized in that; Also be provided with gas liquor inlet on the said pure oxygen non-catalytic partial oxidation stove, the gas liquor inlet on the said pure oxygen non-catalytic partial oxidation stove connects gas liquor through the second gas liquor transfer lime to be separated and treatment system.
17. like claim 15 or 16 described devices; It is characterized in that; Also comprise one first tripping device, said first tripping device is provided with raw gas inlet, raw gas outlet, the outlet of powder ash, and the raw gas inlet on first tripping device connects the first raw gas transfer lime; The raw gas outlet of first tripping device enters the mouth through the raw gas that the second raw gas transfer lime connects said pure oxygen non-catalytic partial oxidation stove, and dust is seen in the powder ash outlet of first tripping device off.
18. device as claimed in claim 17 is characterized in that, said first tripping device is a Cyclonic separating apparatus.
19. device as claimed in claim 17; It is characterized in that; Also comprise a thermal recovery unit; Said thermal recovery unit is provided with high-temperature gas inlet, high-temperature gas outlet, vapour outlet and gas liquor outlet; The high-temperature gas inlet of said thermal recovery unit connects the high-temperature gas outlet on the said pure oxygen non-catalytic partial oxidation stove through the high-temperature gas transfer lime, presses and/or low-pressure saturated steam during the vapour outlet of this thermal recovery unit is seen off, and the gas liquor outlet of thermal recovery unit connects gas liquor through the first gas liquor transfer lime and separates and treatment system; The raw gas that high-temperature gas outlet on the thermal recovery unit is seen off is to produce qualified synthetic gas or hydrogen.
20. device as claimed in claim 17 is characterized in that, the said first gas liquor transfer lime is connected the second gas liquor transfer lime through first connection line with compressor.
21. device as claimed in claim 20; It is characterized in that; Also comprise one second tripping device; Said second tripping device is provided with gas inlet and pneumatic outlet and gas liquor outlet, and the gas inlet on said second tripping device connects the high-temperature gas outlet on the said thermal recovery unit, the raw gas that the pneumatic outlet on second tripping device is seen off through the 3rd raw gas transfer lime; To produce qualified synthetic gas or hydrogen, the gas liquor outlet on second tripping device is connected with the said first gas liquor transfer lime.
22. device as claimed in claim 21 is characterized in that, said second tripping device is the washing Cyclonic separating apparatus.
23. device as claimed in claim 21; It is characterized in that; Also comprise a refrigerating unit; Said refrigerating unit is provided with raw gas inlet, raw gas outlet and gas liquor outlet, and the raw gas inlet on the said refrigerating unit is connected with pneumatic outlet on said second tripping device through pipeline, and the raw gas on the refrigerating unit exports the raw gas of seeing off; To produce qualified synthetic gas or hydrogen, the gas liquor outlet on the refrigerating unit connects gas liquor through the 3rd gas liquor transfer lime and separates and treatment system.
24. device as claimed in claim 23; It is characterized in that; Between said refrigerating unit and said second tripping device, increase by a sulfur-resisting transformation device; Said sulfur-resisting transformation device comprises a heat-exchange equipment and a conversion equipment, and said heat-exchange equipment is provided with raw gas inlet, raw gas outlet, the outlet of conversion gas, conversion gas loop head, and said conversion equipment is provided with raw gas inlet, conversion gas loop exit; Pneumatic outlet on said second tripping device connects the raw gas inlet on the said heat-exchange equipment through the 4th raw gas transfer lime on the one hand, connects the raw gas inlet on the said refrigerating unit through the 5th raw gas transfer lime and valve on the other hand; Conversion gas outlet on the said heat-exchange equipment connects the raw gas inlet on the said refrigerating unit through the conversion letter shoot; Raw gas outlet on the heat-exchange equipment connects the raw gas inlet on the said conversion equipment through the 6th raw gas transfer lime, and the conversion gas loop exit on the conversion equipment connects the conversion gas loop head on the heat-exchange equipment through conversion gas circulation tube.
25. device as claimed in claim 24; It is characterized in that; Also comprise a desulfurization and decarburization device, said desulfurization and decarburization device is provided with raw gas inlet, clean gas outlet and production sulphur or the outlet of vitriolic virgin gas, and the raw gas inlet on the said desulfurization and decarburization device connects the raw gas outlet on the refrigerating unit through the 7th raw gas transfer lime; The purified gas that clean gas outlet on the desulfurization and decarburization device is seen off is to produce qualified synthetic gas or hydrogen; Virgin gas outlet on the said desulfurization and decarburization device is seen off and is produced sulphur or vitriolic virgin gas.
26. device as claimed in claim 25 is characterized in that, said desulfurization and decarburization device is low-temperature rectisol equipment or variable-pressure adsorption equipment.
27. device as claimed in claim 25; It is characterized in that; Also comprise a sulfur recovery unit; Said sulfur recovery unit is provided with virgin gas inlet and sulphur or sulfuric acid outlet, and the virgin gas inlet on the sulfur recovery unit connects the virgin gas outlet on the said desulfurization and decarburization device through the virgin gas transfer lime, and sulphur or sulfuric acid are seen in sulphur on the sulfur recovery unit or sulfuric acid outlet off.
28. device as claimed in claim 27; It is characterized in that; Comprise that also an essence takes off equipment; Said essence is taken off equipment and is provided with purified gas inlet, syngas outlet, and the purified gas inlet that essence is taken off on the equipment connects the clean gas outlet on the desulfurization and decarburization device through the purified gas transfer lime, and the syngas outlet that essence is taken off on the equipment is carried qualified synthetic gas or hydrogen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110247572A CN102320568A (en) | 2011-08-25 | 2011-08-25 | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110247572A CN102320568A (en) | 2011-08-25 | 2011-08-25 | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation |
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| CN102320568A true CN102320568A (en) | 2012-01-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201110247572A Pending CN102320568A (en) | 2011-08-25 | 2011-08-25 | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation |
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| CN103446859A (en) * | 2013-09-12 | 2013-12-18 | 中国海洋石油总公司 | Treatment method of acid gases in coal-made natural gas |
| CN110964575A (en) * | 2019-11-14 | 2020-04-07 | 金沂蒙集团有限公司 | Energy-saving environment-friendly novel synthetic ammonia desulfurization process |
| CN111655825A (en) * | 2018-03-14 | 2020-09-11 | 三菱重工工程株式会社 | Gas refining device |
| CN111717888A (en) * | 2020-06-23 | 2020-09-29 | 山东同智创新能源科技股份有限公司 | Recycling process and system applied to chemical crude ammonia waste gas treatment instead of incineration |
| CN112337410A (en) * | 2020-10-23 | 2021-02-09 | 四川天采科技有限责任公司 | Conversion reactor for methanol hydrogen production and integrated methanol hydrogen production system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103446859A (en) * | 2013-09-12 | 2013-12-18 | 中国海洋石油总公司 | Treatment method of acid gases in coal-made natural gas |
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| CN112337410A (en) * | 2020-10-23 | 2021-02-09 | 四川天采科技有限责任公司 | Conversion reactor for methanol hydrogen production and integrated methanol hydrogen production system |
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Application publication date: 20120118 |