CN204874418U - Coal catalytic gasification system - Google Patents
Coal catalytic gasification system Download PDFInfo
- Publication number
- CN204874418U CN204874418U CN201520346380.4U CN201520346380U CN204874418U CN 204874418 U CN204874418 U CN 204874418U CN 201520346380 U CN201520346380 U CN 201520346380U CN 204874418 U CN204874418 U CN 204874418U
- Authority
- CN
- China
- Prior art keywords
- unit
- pipeline
- type reactor
- storage tank
- catalytic coal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Catalysts (AREA)
Abstract
The utility model relates to a coal catalytic gasification system, including the compounding unit that is used for mixing raw materials coal and catalyst solution, with the dry unit of compounding unit connection, with the gasification unit of dry unit connection and with the sediment ash processing unit of gasification unit connection, the sediment ash processing unit be connected with the salt solution boiler, just the export of the strong brine of salt solution boiler through the pipeline with the compounding unit connection. The utility model discloses not only equipment can be simplified, holistic energy consumption has been reduced moreover.
Description
Technical field
The utility model relates to Coal Gasification Technology field, refers in particular to a kind of catalytic coal gasifaction system.
Background technology
Catalytic coal gasifaction technology is that coal reacts with vaporized chemical at relatively low temperature and generates the higher gasification of effective Gas content under the katalysis of catalyzer.Catalytic coal gasifaction technology is compared with other Coal Gasification Technology, have that gasification rate is high, the advantage such as gasify low (gasification temperature reduces by 200 DEG C ~ 300 DEG C), coal gas easily purify, therefore catalytic coal gasifaction technology is the important way of the clean efficiency utilization of coal, is one of most important and most widely used gordian technique of development Modern Coal-based Chemical.Traditional coal gasification course temperature of reaction is high, generation gas purification difficulty, energy consumption are large, high to equipment requirements, in contrast to this, while the catalytic gasification technology of coal significantly improves gasification reaction speed, also make gasification temperature significantly reduce, the gentleness of coal is gasified and is achieved; Moreover catalytic coal gasifaction technology not only reduces the energy consumption of gasification and the requirement to vapourizing furnace equipment and materials, and is beneficial to desulfurization, the dedusting of gasification, therefore, the catalytic gasification technology of coal is more and more subject to the attention of domestic and international investigator.
At present, the monolithic catalyst that practicality is the strongest is alkali-metal oxyhydroxide or carbonate (normally K
2cO
3), the advantage of this catalyzer be preparation method simple, cheap, can resistance to sulfur poisoning, can high temperature resistant lower sintering and catalyst degradation; And shortcoming is that in gasification, this kind of catalyst levels is larger, the problem that high catalyst addition brings is that high catalyzer cost and a large amount of basic clinkers pollute and emission problem, therefore the recycling of catalyzer becomes the restraining factors of catalytic coal gasifaction large-scale promotion, the research that current catalyst reclaims also is in laboratory stage, does not have the report of industrialization aspect.
In few catalytic coal gasifaction system, reclaim catalyzer normally wash the slag ash of gasification generation and clear up acquisition catalyst lean solution, mix with feed coal again after adopting multiple-effect evaporation that dilute solution is concentrated, the equipment adopting the way of recycling of above-mentioned catalyzer to relate to is many, production of steam conventional in catalytic coal gasifaction flow process and catalyst solution is often utilized to concentrate relevant equipment, as boiler matching multiple-effect evaporator etc., the equipment that above-mentioned production steam and recovery catalyzer need is many, energy consumption is high, is unfavorable for applying.
Utility model content
Problems such as this reason, it is many that technical problem to be solved in the utility model is to overcome the equipment that in prior art, catalyst recovery relates to, and energy consumption is high thus provide one can simplified apparatus, and reduce the catalytic coal gasifaction system of overall power consumption.
For solving the problems of the technologies described above, a kind of catalytic coal gasifaction system described in the utility model, the slag ash processing unit comprising the batch mixing unit for feed coal and catalyst solution being mixed, the drying unit be connected with described batch mixing unit, the gasification unit be connected with described drying unit and be connected with described gasification unit, described slag ash processing unit is connected with salt homogeneous solution-type reactor, and the outlet of the strong brine of described salt homogeneous solution-type reactor is connected with described batch mixing unit by pipeline.
In an embodiment of the present utility model, the clean section of described salt homogeneous solution-type reactor is connected by the steam-in of pipeline with described gasification unit.
In an embodiment of the present utility model, the clean section of described salt homogeneous solution-type reactor is connected by the steam-in of pipeline with described drying unit.
In an embodiment of the present utility model, described slag ash processing unit comprise be connected by pipeline with described gasification unit water washing tank, with the tank connected washing filter of described washing, the dilute solution storage tank be connected with described washing filter, the desiliconization tower be connected with described dilute solution storage tank, the white residue strainer be connected with described desiliconization tower and the desiliconization liquid storage tank that is connected with described white residue strainer.
In an embodiment of the present utility model, described desiliconization liquid storage tank connects ion exchange resin tank.
In an embodiment of the present utility model, described washing filter is also connected successively by pipeline clears up reactor and clear up strainer, described in clear up strainer and connect described dilute solution storage tank by pipeline.
In an embodiment of the present utility model, described washing filter is connected with described reactor of clearing up by transfer roller.
In an embodiment of the present utility model, described water washing tank connects described washing filter, described dilute solution storage tank, described desiliconization tower, described white residue strainer and described desiliconization liquid storage tank successively by pipeline.
In an embodiment of the present utility model, between described salt homogeneous solution-type reactor with described batch mixing unit, be connected catalyst make up tank.
In this embodiment of the present utility model, the outlet of described slag ash processing unit is connected with the drum of pump with described salt homogeneous solution-type reactor by pipeline.
Technique scheme of the present utility model has the following advantages compared to existing technology:
Catalytic coal gasifaction system described in the utility model, adopts salt homogeneous solution-type reactor directly to carry out evaporation concentration to the catalyst lean solution reclaimed, reclaims catalyzer while obtaining steam, not only can simplified apparatus, and reduces overall energy expenditure.
Accompanying drawing explanation
In order to make content of the present utility model be more likely to be clearly understood, below according to specific embodiment of the utility model also by reference to the accompanying drawings, the utility model is described in further detail, wherein
Fig. 1 is the connection diagram of catalytic coal gasifaction system described in the utility model embodiment one;
Fig. 2 is the connection diagram of slag described in the utility model ash processing unit;
Fig. 3 is the connection diagram of catalytic coal gasifaction system described in the utility model embodiment two;
Fig. 4 is the connection diagram of catalytic coal gasifaction system described in the utility model embodiment three;
Fig. 5 is the connection diagram by catalytic coal gasifaction system described in new embodiment four.
Embodiment
Embodiment one
As shown in Figure 1, present embodiments provide a kind of catalytic coal gasifaction system, the slag ash processing unit 14 comprising the batch mixing unit 11 for feed coal and catalyst solution being mixed, the drying unit 12 be connected with described batch mixing unit 11, the gasification unit 13 be connected with described drying unit 12 and be connected with described gasification unit 13, described slag ash processing unit 14 is connected with salt homogeneous solution-type reactor 15, and the outlet of the strong brine of described salt homogeneous solution-type reactor 15 is connected with described batch mixing unit 11 by pipeline.
Catalytic coal gasifaction system described in the utility model, comprise the batch mixing unit 11 for being mixed with catalyst solution by feed coal, the drying unit 12 be connected with described batch mixing unit, the gasification unit 13 be connected with described drying unit 12 and the slag ash processing unit 14 be connected with described gasification unit 13, wherein, described feed coal is transported to described drying unit 12 and dries after mixing in described batch mixing unit 11 with catalyst solution, be transported to described gasification unit 13 more at high temperature to react with vaporized chemical generating gasification, the slag ash of discharging from described gasification unit 13 comprises the coal residue and catalyzer that do not gasify, wherein, major part catalyzer exists with the form of water-soluble cpds, residue small portion is water-insoluble, described slag ash flows into described slag ash processing unit 14 by pipeline, after the process of described slag ash processing unit, obtain catalyst lean solution, described slag ash processing unit 14 is connected with salt homogeneous solution-type reactor 15, and the outlet of the strong brine of described salt homogeneous solution-type reactor 15 is connected with described batch mixing unit 11 by pipeline, described catalyst lean solution forms concentrated catalyst solution by carrying out evaporation concentration in Cemented filling to the drum of described salt homogeneous solution-type reactor 15, described concentrated catalyst solution is discharged by the strong brine relief outlet of described salt homogeneous solution-type reactor 15, and turned back in described batch mixing unit 11 by pipeline and mix with feed coal, thus catalyzer is obtained reclaim, achieve the recycle of catalyzer, significantly save the energy, moreover, by described salt homogeneous solution-type reactor 15, direct for catalyst lean solution evaporation concentration is become concentrated catalyst solution, thus simplify the equipment of whole system, reduce energy expenditure.
In the present embodiment, the drum of described salt homogeneous solution-type reactor 15 is divided into the clean section being positioned at middle part and the salt section being positioned at two ends, the clean section of wherein said salt homogeneous solution-type reactor 15 is connected by the steam-in of pipeline with described gasification unit 13, steam that the clean section of described salt homogeneous solution-type reactor 15 produces is by making steam be reclaimed in Cemented filling to described gasification unit 13, achieve the recycle of steam, be conducive to save energy.
As shown in Figure 2, described slag ash processing unit 14 comprises the water washing tank 141 be connected by pipeline with described gasification unit 13, the washing filter 142 be connected with described water washing tank 141, the dilute solution storage tank 143 be connected with described washing filter 142, the desiliconization tower 144 be connected with described dilute solution storage tank 143, the white residue strainer 145 be connected with described desiliconization tower 144 and the desiliconization liquid storage tank 146 be connected with described white residue strainer 145.Described slag ash is as follows in the treating processes of described slag ash processing unit 14: slag ash carries out pressure washing in described water washing tank 141, water-soluble catalyst is wherein made to enter in water, after washing pulp water by Cemented filling to described washing filter 142, by described washing filter 142 by filtrate by row of conduits to described dilute solution storage tank 143, the catalyst lean solution reclaimed in described dilute solution storage tank 143 is by pipeline and be pumped to described desiliconization tower 144, carries out carbonic acid gas air purge.Because of in described catalyst lean solution containing, ion, these ions need to remove in described desiliconization tower 144, otherwise can be oxidized to ion, catalyst cation such as can exist with, form with these ionic bond, makes described system not possess the function of catalysis coal gasification reaction.CO is passed in described desiliconization tower 144
2ion conversion in solution is H by gas
2s exists in a gaseous form, thus achieves and being separated of liquid state, described and CO
2reaction generates orthosilicic acid Precipitation, the discharge of described desiliconization tower 144 flows into described white residue strainer 145 by pipeline and carries out filtering separation, filtrate and catalyst lean solution are by Cemented filling to described desiliconization liquid storage tank 146, and white residue is discharged through described white residue strainer 145.
In described slag ash processing unit, described washing filter 142 is also connected successively by pipeline to be cleared up reactor 148 and clears up strainer 149, described strainer 149 of clearing up connects described dilute solution storage tank 143 by pipeline, and described washing filter 142 is connected with described reactor 148 of clearing up by transfer roller.Described slag ash is after washing filter 142, clear up reactor 148 described in filter residue transfers to through described transfer roller to clear up, to reclaim insolubility catalyzer in deslagging, described clear up product by row of conduits to described in clear up in strainer 149, deslagging is discharged from described clearing up strainer 149, and filtrate and catalyst lean solution drain in described dilute solution storage tank 143.
In described slag ash processing unit, described desiliconization liquid storage tank 146 connects ion exchange resin tank 147, catalyst lean solution by ion exchange resin tank 147 to remove out calcium, magnesium ion wherein, thus can prevent the formation of dirt in described salt homogeneous solution-type reactor 15 before pumping into described salt homogeneous solution-type reactor 15.
The principle of work of catalytic coal gasifaction system described in the utility model is as follows:
Be transported to described drying unit 12 after being mixed in described batch mixing unit 11 with catalyst solution by feed coal to dry, and then be transported to described gasification unit 13 and at high temperature react with vaporized chemical generating gasification, the slag ash of discharging from described gasification unit 13 comprises the coal residue and catalyzer that do not gasify, described slag ash enters described slag ash processing unit 14, slag ash passes through washing in slag ash processing unit 14, clear up, air purge, catalyst lean solution is obtained after the process such as ion-exchange, described catalyst lean solution by Cemented filling to described salt homogeneous solution-type reactor 15 drum in, carry out evaporation concentration and form concentrated catalyst solution, described concentrated catalyst solution is discharged from the strong brine relief outlet of salt homogeneous solution-type reactor 15, and turn back to batch mixing unit 11 by pipeline and mix with feed coal, thus catalyzer is obtained reclaim, steam that the clean section of described salt homogeneous solution-type reactor 15 produces is by making steam be reclaimed in Cemented filling to gasification unit 13, achieve the recycle of catalyzer and steam simultaneously.
Embodiment two:
As shown in Figure 3, embodiment two is the improvement made on the basis of embodiment one, be from the difference of embodiment one: the steam cycle ingress path that the clean section of described salt homogeneous solution-type reactor 15 produces is different, particularly, the clean section of described salt homogeneous solution-type reactor 15 is connected by the steam-in of pipeline with described drying unit 12, steam that the clean section of described salt homogeneous solution-type reactor 15 produces, by making steam be reclaimed in Cemented filling to described drying unit 12, achieves the recycle of steam, is conducive to save energy.
Embodiment three:
As shown in Figure 4, embodiment three is the improvement made on the basis of embodiment one or embodiment two, be from the difference of embodiment one or embodiment two: the steam cycle ingress path that the clean section of described salt homogeneous solution-type reactor 15 produces is different, particularly, the clean section of described salt homogeneous solution-type reactor 15 is connected by the steam-in of pipeline with described gasification unit 13, simultaneously, the clean section of described salt homogeneous solution-type reactor 15 is also connected with the steam-in of described drying unit 12 by pipeline, namely the steam that the clean section of described salt homogeneous solution-type reactor 15 produces can be delivered to described gasification unit 13 by pipeline, also can be delivered in described drying unit 12 thus steam is reclaimed, achieve the recycle of steam, thus save energy to the full extent.
Embodiment four
As shown in Figure 5, the present embodiment is in embodiment one, embodiment two, the improvement in embodiment three, any one embodiment made, be provided in described batch mixing unit 11 to mix with described feed coal and be beneficial to generating gasification in described gasification unit 13 to make the concentrated catalyst solution evaporated from described salt homogeneous solution-type reactor 15 and react, particularly, catalyst make up tank 16 is connected between described salt homogeneous solution-type reactor 15 with described batch mixing unit 11, direct for catalyst lean solution evaporation concentration is become concentrated catalyst solution by described salt homogeneous solution-type reactor 15, catalyzer strong solution to turn back between described batch mixing unit 11 and in catalyst make up tank, 16 can supplement a small amount of catalyzer.
To sum up, above technical scheme described in the utility model has the following advantages:
1. catalytic coal gasifaction system described in the utility model, becomes concentrated catalyst solution by described salt homogeneous solution-type reactor by direct for catalyst lean solution evaporation concentration, thus simplifies the equipment of whole system, reduces energy expenditure; Moreover, achieve the recycle of catalyzer and steam, significantly save the energy.
2. in slag ash processing unit described in the utility model, described desiliconization liquid storage tank connects ion exchange resin tank, catalyst lean solution by ion exchange resin tank to remove out calcium, magnesium ion wherein, thus can prevent the formation of dirt in described salt homogeneous solution-type reactor before pumping into described salt homogeneous solution-type reactor.
Obviously, above-described embodiment is only for clearly example being described, the restriction not to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And thus the apparent change of extending out or variation be still in the protection domain that the utility model creates.
Claims (10)
1. a catalytic coal gasifaction system, the slag ash processing unit comprising the batch mixing unit for feed coal and catalyst solution being mixed, the drying unit be connected with described batch mixing unit, the gasification unit be connected with described drying unit and be connected with described gasification unit, it is characterized in that: described slag ash processing unit is connected with salt homogeneous solution-type reactor, and the outlet of the strong brine of described salt homogeneous solution-type reactor is connected with described batch mixing unit by pipeline.
2. catalytic coal gasifaction system according to claim 1, is characterized in that: the clean section of described salt homogeneous solution-type reactor is connected by the steam-in of pipeline with described gasification unit.
3. catalytic coal gasifaction system according to claim 1 and 2, is characterized in that: the clean section of described salt homogeneous solution-type reactor is connected by the steam-in of pipeline with described drying unit.
4. catalytic coal gasifaction system according to claim 1, is characterized in that: described slag ash processing unit comprise be connected by pipeline with described gasification unit water washing tank, with the tank connected washing filter of described washing, the dilute solution storage tank be connected with described washing filter, the desiliconization tower be connected with described dilute solution storage tank, the white residue strainer be connected with described desiliconization tower and the desiliconization liquid storage tank that is connected with described white residue strainer.
5. catalytic coal gasifaction system according to claim 4, is characterized in that: described desiliconization liquid storage tank connects ion exchange resin tank.
6. catalytic coal gasifaction system according to claim 4, is characterized in that: described washing filter is also connected successively by pipeline clears up reactor and clear up strainer, described in clear up strainer and connect described dilute solution storage tank by pipeline.
7. catalytic coal gasifaction system according to claim 6, is characterized in that: described washing filter is connected with described reactor of clearing up by transfer roller.
8. catalytic coal gasifaction system according to claim 4, is characterized in that: described water washing tank connects described washing filter, described dilute solution storage tank, described desiliconization tower, described white residue strainer and described desiliconization liquid storage tank successively by pipeline.
9. catalytic coal gasifaction system according to claim 1, is characterized in that: be connected catalyst make up tank between described salt homogeneous solution-type reactor with described batch mixing unit.
10. catalytic coal gasifaction system according to claim 1, is characterized in that: the outlet of described slag ash processing unit is connected with the drum of pump with described salt homogeneous solution-type reactor by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520346380.4U CN204874418U (en) | 2015-05-26 | 2015-05-26 | Coal catalytic gasification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520346380.4U CN204874418U (en) | 2015-05-26 | 2015-05-26 | Coal catalytic gasification system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204874418U true CN204874418U (en) | 2015-12-16 |
Family
ID=54818815
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520346380.4U Active CN204874418U (en) | 2015-05-26 | 2015-05-26 | Coal catalytic gasification system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204874418U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106085508A (en) * | 2016-06-02 | 2016-11-09 | 新奥科技发展有限公司 | A kind of catalytic coal gasifaction method |
| CN111321013A (en) * | 2020-03-09 | 2020-06-23 | 新奥科技发展有限公司 | Coal catalytic gasification method and system |
| CN114042464A (en) * | 2021-11-03 | 2022-02-15 | 新奥科技发展有限公司 | Salt-containing wastewater catalyst and method for catalyzing coal gasification reaction by using same |
-
2015
- 2015-05-26 CN CN201520346380.4U patent/CN204874418U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106085508A (en) * | 2016-06-02 | 2016-11-09 | 新奥科技发展有限公司 | A kind of catalytic coal gasifaction method |
| CN111321013A (en) * | 2020-03-09 | 2020-06-23 | 新奥科技发展有限公司 | Coal catalytic gasification method and system |
| CN114042464A (en) * | 2021-11-03 | 2022-02-15 | 新奥科技发展有限公司 | Salt-containing wastewater catalyst and method for catalyzing coal gasification reaction by using same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102886199B (en) | Flue gas desulfurization device and desulfurization method by magnesium oxide process | |
| CN103523945A (en) | Clean production method of plant fiber product | |
| CN204874418U (en) | Coal catalytic gasification system | |
| CN203436980U (en) | Device for treating waste gas in diammonium phosphate production | |
| CN101659889B (en) | Methane purifying comprehensive utilization technology | |
| CN104086011B (en) | Be applicable to the technique of zero discharge of viscose fibre industry acid station waste water | |
| CN113772884A (en) | Coking wastewater treatment system and method | |
| CN112358047A (en) | System and process for supplementing carbon source of sewage plant by using aquatic plants | |
| CN111603903A (en) | Double-alkali desulphurization device | |
| CN103691294A (en) | Device and technology for wet-type double-alkali method-based desulphurization and dedusting | |
| CN110776131A (en) | Zero-discharge system and process for regenerated wastewater of condensate fine treatment system of coal-fired power plant | |
| CN101323441B (en) | Reclaiming method of wet method phosphoric acid ardealite storage yard eluviate water | |
| CN104437062A (en) | Device and method for recovering phosphoric acid from phosphoric-acid-method activated carbon tail gas | |
| CN109336074A (en) | The method of aluminium industry polished and cleaned Sewage treatment compound fertilizer | |
| CN209113673U (en) | A kind of water-saving dry coal powder pressure gasifying usage on black water device | |
| CN209890418U (en) | Ammonia-soda process ammonia distillation waste liquid resource utilization system | |
| CN202010512U (en) | Flue gas desulfuration device of non-ferrous metal processing waste liquid management coal-water slurry boiler | |
| CN209161720U (en) | A kind of desulfurization wastewater recycling and zero discharge system | |
| CN206927636U (en) | A kind of dehydrogenation of isobutane device waste water reclaiming device | |
| CN112125439A (en) | System for removing fluorine ions in wastewater for coal gas production | |
| CN206219295U (en) | A kind of Texaco gasifier buck high efficient resourcing recycling system | |
| CN204417131U (en) | A kind of device for reclaiming phosphoric acid in activated carbon of phosphoric acid method tail gas | |
| CN206219346U (en) | A kind of Texaco gasifier buck resource utilization system | |
| CN201420025Y (en) | Continuous production system for producing nano and active zinc oxide by ammonia process | |
| CN109179843A (en) | A kind of water-saving dry coal powder pressure gasifying usage on black water device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170203 Address after: 065001 Hebei economic and Technological Development Zone, Langfang science and Technology Park in the Southern District of B building, room 522 Patentee after: ENN SCIENCE & TECHNOLOGY DEVELOPMENT Co.,Ltd. Address before: The 065001 Hebei economic and Technological Development Zone of Langfang Huaxiang Xinyuan host new Austrian Science and Technology Park in Southern District Patentee before: ENN Coal Gasification Co., Ltd. |