CN103805280A - Gasification system for solid fuel - Google Patents
Gasification system for solid fuel Download PDFInfo
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- CN103805280A CN103805280A CN201310524643.1A CN201310524643A CN103805280A CN 103805280 A CN103805280 A CN 103805280A CN 201310524643 A CN201310524643 A CN 201310524643A CN 103805280 A CN103805280 A CN 103805280A
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Abstract
An object is to suppress energy efficiency reduction due to fuel drying and to effectively utilize steam generated through fuel drying in a gasification system using lignite or 5 another high-moisture solid fuel. A high-moisture solid fuel having a high moisture content is dried upstream from a gasifier. The high-moisture solid fuel after drying is fed to the gasifier to thereby prevent temperature fall in the gasifier. A steam-containing gas evolved through fuel drying is fed to 10 downstream from the gasifier, cools the syngas, and accelerates the shift reaction. Examples of the fuel-drying heat source include steam generated through heat recovery downstream from the shift reactor; plant exhaust heat derived typically from steam used for regenerative heating of a CO 2 15 absorbing liquid in a CO 2 regeneration tower; and CO 2 adiabatically compressed after being recovered from the syngas.
Description
Technical field
The present invention relates to the solid-fuelled gasification system that uses the moisture amounts such as brown coal higher, relate to reducing by the solid-fuelled dry efficiency causing the system suppressing.
Background technology
The solid-fuelled utilization of the high-moistures such as brown coal increases to the roughly half of the utilization of coal entirety.The moisture amount of brown coal is 30～65% left and right.These data are higher 5～10 times than the bituminous coal of more use in Japan's generating is used.The net thermal value of the per unit weight of brown coal is 40～70% left and right of bituminous coal, and therefore the temperature of combustion of the brown coal under identical oxygen content will low hundreds of degree compared with bituminous coal.
On the other hand, make Ministry of Coal Industry's divided combustion (gasification) and reclaiming with CO, H
2carry out slag from generating the coal gasifier of gas delivery, more than temperature in stove need to being increased to ash fusion point (1200～1600 ℃) for the generation gas of principal constituent and by the ash content in coal.In the situation that brown coal are directly put into vapourizing furnace, because its amount of moisture is large and net thermal value is lower, cannot make temperature in stove raise, exist and in stove, can not carry out grey melting and the situation of the running of cannot gasifying.In order to improve temperature in stove, the brown coal drying before need in advance vapourizing furnace being dropped into reduces amount of moisture, improves net thermal value.
In addition, in order to improve gasification system entirety efficiency, need to seek for the energy usage reduction of brown coal drying and effective utilization of the water vapour producing.For example, in patent documentation 1, record following brown coal drying system: use fluidised bed in brown coal dry, is applied to three kinds of following situations by the water vapour of generation.
(1) make water vapour recirculation fluidization gas and direct-fired thermal source as brown coal in fluidised bed.
(2) the new water vapour recovery of heat that comes from water vapour being produced is used as the thermal source of the brown coal indirect heating in fluidised bed.
(3) water vapour is used as to the transformationreation steam in shift-converter.
In addition, in patent documentation 2, disclose following gasification system: the upstream that the subbituminous coal for making the moisture with regulation or brown coal drying is formed to drying installation that amount of moisture regulates coal and be located at coal gasification reaction stove, the amount of moisture that generation has the amount of moisture of regulation regulates coal, does not supply with water vapour by tar/coke high-efficiency gasification to vapourizing furnace.
Formerly technical literature
Patent documentation
Patent documentation 1: TOHKEMY 2011-214562 communique
Patent documentation 2:WO International Publication 2011-129192 communique
The problem that invention will solve
Before the solid fuel that makes the high-moistures such as brown coal drops into vapourizing furnace, carry out in dry gasification system, in order to improve the efficiency of entire system, need to reduce the energy usage dry for fuel and effectively utilize the water vapour producing.
First, an example of the energy usage tentative calculation in dry as fuel, contains moisture 750t/d using the high-moisture solid fuel 1500t/d(to moisture 50wt%) be dried, contain moisture 250t/d as the high-moisture solid fuel 1000t/d(of moisture 25wt%) and put into total calorific value in the situation of vapourizing furnace, dried fuel and be illustrated in table 1.In addition, dry fuel needed calorimeter is shown in table 2.
In table 2, suppose that the moisture in fuel exists as the liquid of 20 ℃, the dry definition of fuel is the water of the liquid of 20 ℃ to be heated into the water vapour of 100 ℃.
Known according to (4) of table 1 (the Giga Joule of unit) and (10) of table 2, the dry needed heat of fuel reach dry after fuel total calorific value about 7%.At this, the dry thermal source of fuel can be more than 100 ℃, and the used heat utilization that gasification system produces is effective.In addition, at the CO possessing in generation gas
2in the gasification system of recovering mechanism, also consider the CO to reclaiming
2heat and set it as the system of the dry thermal source of fuel.But, in patent documentation 1, for the used heat, the recovery CO that use gasification system
2carry out the dry gasification system of fuel, do not mention.
[table 1]
An example of the total calorific value tentative calculation of fuel after dry
（1000t/d）
| Project | Unit | Numerical value | Remarks |
| (1) dried fuel quantity | t/d | 1000 | 1500t/d before dry |
| (2) whole moisture | wt% | 25 | 50wt% before dry |
| (3) net thermal value | kJ/kg | 18600 | ? |
| (4) total calorific value of dry rear fuel | GJ/d | 18600 | （1）×（3） |
[table 2]
One example of the dry needed heat tentative calculation of fuel
(fuel 1500t/d(moisture 50wt% before dry) → 1000t/d(moisture 25wt%))
| Project | Unit | Numerical value | Remarks | |
| (5) vaporize water component | t/d | 500 | According to (1), (2) | |
| (6) dry | ℃ | 20 | Liquid | |
| (7) dry rear temperature | ℃ | 100 | Water vapour | |
| (8) water specific heat | kJ/kg | 4.2 | ? | |
| (9) evaporation potential | kJ/kg | 2256 | ? | |
| (10) the dry needed heat of fuel | GJ/d | 1296 | The water vapour of water → 100 of 20 ℃ ℃ |
Next, as by the dry water vapour producing of fuel effectively utilize method, consider the conversion of the steam that the fluidization medium dry to generating, fuel or drying source, gasification system use.If the dry fuel water vapour producing is made as under normal pressure to 100 ℃, the vapour temperature significantly using lower than thermal power generation etc. (more than 500 ℃) and pressure (more than 20MPa), efficiency is not good.In addition, in the case of as the dry fluidization medium of fuel, drying source, the water vapour of generation finally all reclaims as water, therefore needs drain treatment apparatus.
Based on above reason, preferably the dry fuel water vapour conversion producing is made to steam that gasification system uses, and by system corresponding to existing water treatment device.Therefore,, as the purposes of the dry water vapour producing of fuel, be preferred for generating gas cooling and use with CO transformationreation and use.
In patent documentation 1, there is the record relevant to the system that the dry fuel water vapour producing is used as to the CO transformationreation steam in CO shift-converter, but for the system that this water vapour is dropped into generation gas cooling portion, do not record.
In addition, in patent documentation 2, it is effective supplying with water vapour and make to become the decomposition of water vapour enrichment atmosphere STRENGTH ON COKE in thermolysis gasification reacting furnace from steam jet, if but steam vapour amount increase the temperature in gasification reacting furnace reduce and speed of response reduced, and need a locking equipment, therefore disclose and utilized amount of moisture to regulate the moisture of coal to carry out the new gasification system of coke decomposition etc.But, in patent documentation 2, do not find and suitably supply with water vapour to gasification reacting furnace and carry out the record that the gasification system of processing of the water vapour of discharging in the drying process of brown coal etc. is relevant.
Summary of the invention
For solving the means of problem
The present invention is a kind of solid-fuelled gasification system, wherein, this gasification system possesses: solid-fuelled hopper, fuel carrying loop, vapourizing furnace, generation gas cooling portion, cleaning apparatus, washing tower and desulfurizer after drying installation dry solid fuel, dried solid-fuelled shredding unit, storage are pulverized, the gas that contains water vapour that will produce at described drying installation mix with the generation gas that comes from described vapourizing furnace in the downstream side of described vapourizing furnace.
The present invention makes to generate gas in the generation gas cooling portion in vapourizing furnace downstream with high temperature by the dry water vapour producing of fuel and mixes, and seeks to realize the cooling and CO transformationreation promotion that generates gas simultaneously.Generating gas cooling portion as long as adopt, only make the water vapour of 100 ℃ boost and just can drop into, is therefore the most promising as the purposes of the water vapour by the dry generation of fuel.
Solid fuel more moisture amount is dried at the upstream side of vapourizing furnace, dried solid fuel is supplied with to vapourizing furnace.On the other hand, make to be supplied with to the downstream of vapourizing furnace by the dry gas that contains water vapour producing of fuel and with generate gas and mix, carry out cooling and promote CO transformationreation generating gas.In addition supply with to shift-converter with steam the remainder of the gas that contains water vapour as transformationreation.
In the dry thermal source of fuel, utilize the used heat being produced by gasification system.At the CO possessing in generation gas
2in the situation of the system of recovering mechanism, the water vapour that produces by the generation gas by CO shift-converter high temperature, at the heat recovery section place in CO shift-converter downstream, by CO
2regenerator column carries out CO
2the regeneration of absorption liquid adds the water vapour of hankering using as thermal source.In addition, to the CO reclaiming
2carry out heat insulation compression, by the CO of high temperature
2carry out fuel as thermal source and be dried, utilize this CO
2dried solid fuel is transported to vapourizing furnace.
Fuel is dry mainly to be implemented by moisture eliminator, but also can make to boost by locking hopper, fuel in standby is dried.The period of storage of the fuel at locking hopper place is at least more than 20 minutes, by transporting medium is put in locking hopper and boosted.Thereby, by by the CO of described heat insulation compression high temperature
2put into locking hopper, thus can be at locking hopper inner drying fuel.
Invention effect
According to the present invention, make to be mixed and cooling generation gas with generation gas in the downstream of vapourizing furnace by the dry water vapour producing of fuel, and promote CO transformationreation at the leading portion of shift-converter.Thus, make to generate the miniaturization of gas cooling portion, and reduce the usage quantity of the transformationreation steam that CO shift-converter uses.In addition, as the dry thermal source of the fuel in drying installation, use at the unnecessary water vapour of the heat recovery section place in CO shift-converter downstream generation, at CO,
2regenerator column place is for CO
2water vapour after the regeneration heating of absorption liquid etc., the equipment used heat that do not utilize in the past, thereby suppress to be reduced by the dry efficiency causing of fuel.
Accompanying drawing explanation
Fig. 1 is the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 1.
Fig. 2 is the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 2.
Fig. 3 is the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 3.
Fig. 4 is the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 4.
Embodiment
Below, based on illustrated embodiment, the gasification system of high-moisture solid fuel of the present invention is described.
[embodiment 1]
Fig. 1 is the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 1.The gasification system of the high-moisture solid fuel of embodiment 1 possesses drying installation, shift-converter and the CO of high-moisture solid fuel
2recovering mechanism, uses respectively at the thermal source place of drying installation the generation gas by transformationreation high temperature and reclaims CO
2a part carry out heat insulation compression and the CO of high temperature
2sensible heat.
The moisture amount of the high-moisture solid fuels such as brown coal 1 reaches 30～65wt%, and in using than Japan's generating, widely used bituminous coal is high 5～10 times.The thermal value of the per unit weight of the high-moisture solid fuels such as brown coal 1 is also lower, is therefore difficult to directly drop into vapourizing furnace 16.This is because cannot make temperature rise in stove, and can not carry out the stable discharge of grey melting and slag.
Therefore, first high-moisture solid fuel 1 is dried by drying installation 2, pulverizes by shredding unit 3.Afterwards, identical with the gasification system of existing bituminous coal etc., be stored in locking hopper 4, transfer to hopper 5 via transferring valve 6, supply with to vapourizing furnace GF via carrying pipe 10.
Vapourizing furnace GF is by gasification portion 16 and generate gas cooling portion 18 and form, and is also supplied to by air trap 13 from the isolated oxygen 15 of air 11 in gasification portion 16, and high-moisture solid fuel 1 gasifies in stove, produces the generation gas 17 of high temperature.Meanwhile, under the high temperature atmosphere of the ash content in fuel in stove, carry out melting, separate from generating gas 17 as slag.Sometimes generate gas 17 and reach more than 1000 ℃ in gasification portion 16 exits, be also attended by coke 20, be cooled to 400 ℃ of less thaies by generating gas cooling portion 18.Generate gas 17 and carry out dedusting at cleaning apparatus 19 places that are arranged at the downstream that generates gas cooling portion 18.At this, the coke of recovery 20 is put into vapourizing furnace 16 again, again gasify.
The generation gas 17 that carried out dedusting by cleaning apparatus 19 is cooled to 100 ℃ of left and right at washing tower 33 places, and to remove halogen be material, minute dust, carries out desulfurization by thionizer 34.Generation gas 35 after the desulfurization of 40 ℃ of left and right is heated to more than 200 ℃ with the well heater 37 that generates gas by the interchanger 36 that generates gas, supplies with to shift-converter.Transformationreation refers to the reaction shown in formula (1), in the time carrying out to right, is thermopositive reaction.
CO＋H
2O→CO
2＋H
2……（1）
Transformationreation is carried out actively above at 1000 ℃ under catalyst-free, but utilizes transformation catalyst also can react actively below at 500 ℃.The Heating temperature of the generation gas 35 after desulfurization is determined by the active temperature that is filled into the catalyzer in shift-converter.
In addition, shift-converter is provided with many conventionally, reclaims reaction heat by the downstream side at shift-converter, the temperature in shift-converter is kept within the limits prescribed to protection transformation catalyst.In embodiment 1, the situation that two shift-converters are arranged in the mode of series connection represents as an example, is called the first shift-converter 38, the second shift-converter 54 from upstream side.
At CO
2absorption tower 42 has absorbed CO
2cO
2absorption liquid 47 is heated to more than 100 ℃, to CO by interchanger 44, well heater 45
2 regenerator column 46 is supplied with.At CO
2regenerator column 46 discharges and has absorbed CO
2cO
2cO in absorption liquid 47
2thereby, can realize CO
2the recycling of absorption liquid 47.
Pass through CO
2the recovery CO that regenerator column 46 reclaims
2a part of 101 becomes recycling CO
2102, remainder becomes stores CO
2103.Recycling CO
2102 flow is by recycling CO
2 flow control valve 51 adjust.At recycling CO
2in 102, the CO being discharged by gasification system
2(figure Zhong ﹡ b, ﹡ c, ﹡ e) also can with store CO
2103 mix, and are stored in inferior.
In order to guarantee CO compared with highland
2the CO at regenerator column 46 places
2the rate of recovery, need to be incubated absorption liquid.Therefore, can extract the CO of a part of absorption liquid as regeneration heating use out
2 absorption liquid 48, is passing through CO
2the well heater 49 of absorption liquid reheat 100 ℃ above after, turn back to CO
2regenerator column 46.In the thermal source of this regeneration heating, be suitable for the low-temperature steam of 150～300 ℃ of left and right, call it as CO
2the regeneration of absorption liquid steam 50 for heating.
At this, in embodiment 1, record, at the CO of the generation gas 41 from after transformationreation
2in recovery, use the chemical absorption mode of absorption liquid, but also can use physical absorption, chemical absorption, absorption, membrane sepn, other such CO of low temperature separation process mode
2way of recycling.
Next, carry out the moisture amount of dried high-moisture solid fuel by described drying installation 2, expect to be made as below 25wt% based on fuel character.If in advance moisture amount is dried to this degree, can utilize the treatment process identical with bituminous coal to pulverize.Comminuted, the interior temperature of vapourizing furnace that dried moisture amount is considered, can pre-determine according to the kind of each coal.
The contained moisture of brown coal can be thought and is the liquid particle that is adsorbed in.In order to make the moisture drying in brown coal, liquid water is heated to 100 ℃, make its evaporation and become water vapour.On the other hand, brown coal, compared with bituminous coal, have the feature of easy spontaneous combustion, under air atmosphere 150 ℃ of danger above with spontaneous combustion.In sum, the temperature of drying source need to be made as more than 100 ℃, utilize the gas that does not contain oxygen by the seal inside of drying installation 2, reduce in advance oxygen concentration.As the gas that does not contain oxygen that can use in the present embodiment, can expect CO
2, nitrogen, water vapour, argon gas, but use the situation of high-temperature gas comparatively favourable, so preferred CO
2or water vapour.
In addition, as described in Table 2, produce a large amount of water vapour by drying installation 2.By utilizing this water vapour, the steam that can carry out without the recovery of heat in the gasification system by existing (bituminous coal etc.) produces operation, and by the heat at this operation place is used as to drying source, can build reducing by the dry efficiency causing of fuel the gasification system suppressing.
In embodiment 1, represent following gasification system, this gasification system is compressed the water vapour being produced by drying installation 2 and boosts to and the pressure equal extent of gasification portion 16 water vapour 40 for cooling and transformationreation of the generation gas 17 producing for gasification portion 16 by compressor 28.
In existing gasification system, transformationreation is main in the downstream of shift-converter, using transformationreation heat as thermal source with water vapour 40.But, if by the gas that contains water vapour being produced by drying installation 27 as water vapour 40 for transformationreation, for example in the downstream of the first shift-converter 38, the heat of the generation gas 53 by transformationreation high temperature becomes residue.
Therefore, the generation gas 53 by transformationreation high temperature can be supplied with to drying installation 2, the sensible heat of the generation gas 53 by transformationreation high temperature is used as to drying source.The temperature of the generation gas 53 by transformationreation high temperature, more than 200 ℃, is therefore suitable as drying source.It should be noted that, this temperature changes according to the active temperature of catalyst for water-gas shift reaction, occupied state.
On the other hand, the method for cooling of the generation gas 17 in above-mentioned generation gas cooling portion 18 is:
(a) heat exchange of the steam and in heat pipe etc.
(b) spraying of spray water 32
(c) generate gas cooling portion, with mixing that the gas 29 that contains water vapour carries out.
In the gasification system of high-moisture solid fuel 1, can utilize (c), therefore can make to generate 18 miniaturizations of gas cooling portion, cut down the flow of spray water 32.Generating in gas cooling portion 18, in the case of making the gas that contains water vapour of (c) mixes with more than 1000 ℃ generation gas 17, the transformationreation of formula (1) is carried out under the condition of catalyst-free.
Thus, can reduce the usage quantity of the transformationreation water vapour 40 of shift-converter input downstream.In addition, also can reclaim useful hydrogen from the gas 27 dry generation by high-moisture solid fuel 1, that contain water vapour, effectively utilize the moisture of high-moisture solid fuel 1.(c) flow is subject to the flow restriction of the spray water of gas composition, (b) at washing tower 33 places in downstream, therefore needs to arrange flow control valve 31.
On the other hand, the in the situation that of above-mentioned table 2, the gas that contains water vapour 30 of supplying with to shift-converter can be received the whole amount of gas 27 that contains water vapour.This is because use under the condition that transformationreation (also exists the situation that approaches twice) with water vapour 40 more than stoichiometric ratio.Therefore, do not need flow control valve, as long as there is the well heater 39 of the gas that contains water vapour for being heated to the temperature that is applicable to transformationreation.
In addition,, in embodiment 1, as the non-active gas that dried high-moisture solid fuel and coke 20 are carried, use the CO being reclaimed by native system
2a part.To reclaim CO
2a part of 101 is as recycling CO
2102 carry out branch, pass through CO
2compressor 52 carries out heat insulation compression and boosts, heats up, and will compress CO
2104 supply with to drying installation 2.This is because use compression CO in the drying source in drying installation 2
2104 sensible heat.For example,, if by the CO of normal temperature, normal pressure
2be compressed to 10MPa, can be warming up to about 100 ℃.
The CO discharging from drying installation 2
2a part supply with to locking hopper 4, hopper 5 and coke locking hopper 21, the coke feed bucket 22 of dried high-moisture solid fuel as transporting medium, to vapourizing furnace, GF supplies with.The CO that transporting medium uses
2flow by transporting medium CO
2 flow control valve 60 adjust.
In sum, embodiment 1 not only can coolingly be made to generate gas cooling portion and realize miniaturization by what the dry gas that contains water vapour producing by high-moisture solid fuel was generated to gas for high temperature, the transformationreation promotion under catalyst-free condition can also be passed through and the moisture recover hydrogen from fuel, and the water vapour usage quantity of the shift-converter in downstream can be reduced.
In addition, by the gas that contains remaining water vapour being applied flexibly to the transformationreation steam of doing in shift-converter, can significantly reduce from the outside transformationreation vapor volume of supplying with of system.
In addition, by by become this thermal source the generation gas by transformationreation high temperature sensible heat and to reclaim CO
2a part carry out heat insulation compression and the CO of high temperature
2sensible heat as the drying source of high-moisture solid fuel, thereby can build the gasification system that suppresses to reduce and effectively utilize by the dry efficiency causing of fuel the moisture of high-moisture solid fuel.
[embodiment 2]
In Fig. 2, represent the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 2.In embodiment 2, in embodiment 1 with above-mentioned Fig. 1 difference, the drying source that utilizes method and drying installation 2 of the sensible heat of the generation gas 53 by transformationreation high temperature describes.
In embodiment 2, reset the conversion interchanger 55 of the sensible heat of the generation gas 53 for reclaiming the transformationreation high temperature by producing from the first shift-converter 38.In conversion interchanger 55, utilize this sensible heat that water vapour is heated to more than 200 ℃, as high-moisture solid fuel 1 dry with water vapour 56 and transformationreation water vapour 40 and make it feed back and be used to the first shift-converter 38, the second shift-converter 54.Transformationreation is corresponding with the flow of the gas that contains water vapour 30 of supplying with to shift-converter that comes from drying installation 2 with the flow of water vapour 40, uses the flow control valve 57 of water vapour to adjust by transformationreation.
Be heated to 200 ℃ of above are dryly directed in drying installation 2 with water vapour 56, be dried high-moisture solid fuel 1 by its sensible heat.In Fig. 2, by indirect heat exchange mode, high-moisture solid fuel 1 is heated with water vapour 56 by dry, be supplied to direct heat exchange mode drying installation 2 in by being dried with part or all of water vapour 56 but also can adopt.
That discharges from drying installation 2 has dryly carried out mixing from the outside supply steam 58 coming of supplying with of system of flow adjustment with water vapour 56 and the flow control valve 59 by supply steam, is again heated to more than 200 ℃ by conversion interchanger 55.
In sum, utilization is used as to drying source and the transformationreation water vapour of high-moisture solid fuel by the warmed-up water vapour of sensible heat of the generation gas of transformationreation high temperature, thereby can builds the gasification system that suppresses to reduce and effectively utilize by the dry efficiency causing of fuel the moisture of high-moisture solid fuel.
[embodiment 3]
In Fig. 3, represent the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 3.In embodiment 3, in embodiment 2 with above-mentioned Fig. 2 difference, be about to dry with water vapour 56 also as the CO of regeneration heating use
2the gasification system of the heat source of absorption liquid 48 describes.
To be heated to 200 ℃ of above dry water vapour 56 of using by conversion interchanger 55 to CO
2the well heater 49 of absorption liquid is supplied with.Thus, by the CO of regeneration heating use
2absorption liquid 48 is heated to more than 100 ℃.On the other hand, by dryly supplying with to drying installation 2 with the state maintaining more than 100 ℃ with water vapour 56 of discharging from well heater 49, become the drying source of high-moisture solid fuel 1.
The dry temperature with water vapour 56 of the entrance of drying installation 2 is lower than the situation of embodiment 2, and the dry sensible heat with water vapour 56 that therefore can utilize at drying installation 2 also tails off.Therefore,, in order not use the outer thermal source of thermally guaranteeing drying installation 2, can consider following three countermeasures.
Countermeasure 1 is to increase heat insulation compression CO
2(104) flow.
In sum, will utilize by the warmed-up water vapour of sensible heat being dried and CO as high-moisture solid fuel of the generation gas of transformationreation high temperature
2the thermal source reheating of absorption liquid and transformationreation water vapour, can build the gasification system that suppresses to be reduced and effectively utilized by the dry efficiency causing of fuel the moisture of high-moisture solid fuel.
[embodiment 4]
In Fig. 4, represent the loop diagram of the gasification system of the high-moisture solid fuel of embodiments of the invention 4.In embodiment 4, in embodiment 3 with above-mentioned Fig. 3 difference, by heat insulation compression CO
2104 to the hopper of storing, carry dried high-moisture solid fuel supply with, by dried high-moisture solid fuel further system dry and that carry out preheating describe.
To compress CO
2104 not only to drying installation 2, also to the locking hopper 4 that dried high-moisture solid fuel is stored, boosted, the hopper of its storage 5 is supplied with for carrying under pressurized state.Locking hopper 4 is boosted and move to standby time till hopper 5 depending on hopper capacity, at least more than 20～30 minutes.In locking hopper 4, by using the compression CO as the high temperature of transporting medium
2104 supply with and boost, and can further be dried high-moisture solid fuel.By by this CO
2also supply with and as the transporting medium that leads to vapourizing furnace, also can carry out preheating to high-moisture solid fuel to hopper 5.
From locking hopper 4, discharge and contain CO via locking hopper equalizing valve 7, pressure regulator valve 9
2with the gas (﹡ of water vapour b).Contain CO
2b) can generate gas cooling portion 18 for generating the cooling of gas 17 with the gas (﹡ of water vapour.Containing CO
2with the gas of water vapour (﹡ b) in also containing fine-grained solids, this solids can reclaim by existing cleaning apparatus 19.
In addition, in the inside of drying installation 2, supply with the gas that does not contain oxygen 61 of high temperature, promote the heating of high-moisture solid fuel 1.As the gas that does not contain oxygen 61 of high temperature, preferably water steam, CO
2.
Now, the gas that contains water vapour 27 producing from drying installation 2, likely containing fine-grained solids.If this solids is supplied with to shift-converter, likely make transformationreation reduce, make transformation catalyst generation deteriorated.Therefore, the cleaning apparatus 62 of the gas that contains water vapour of supplying with to shift-converter is set, reclaims the solids 63 that disperses.The solids 63 that disperses can be supplied to vapourizing furnace 16 from coke locking hopper 21 together with coke 20.
In sum, by heat insulation compression CO
2supply with to locking hopper, use boost, standby time and make high-moisture solid fuel dry, thereby also can realize the miniaturization of drying installation.In addition, by by heat insulation compression CO
2also supply with to hopper, can carry out preheating to high-moisture solid fuel and transporting medium, therefore also become and be suppressed at the countermeasure that in the stove that the vapourizing furnace of high-moisture solid fuel worries, temperature reduces.
Industrial applicibility
The present invention can be used in the gasification system of the high-moisture solid fuel of the high-moistures such as brown coal.
Description of reference numerals:
1 ... high-moisture solid fuel
2 ... drying installation
3 ... shredding unit
4 ... locking hopper
5 ... hopper
6 ... transfer valve
9 ... pressure regulator valve
10 ... carrying pipe
11 ... air
12 ... compressor
13 ... air trap
14 ... nitrogen
15 ... oxygen
16 ... gasification portion
17 ... generate gas
18 ... generate gas cooling portion
19 ... cleaning apparatus
27,29,30 ... the gas that contains water vapour
28 ... compressor
31,51 ... flow control valve
32 ... spray water
33 ... washing tower
34 ... desulfurizer
35 ... generation gas after desulfurization
36,44 ... interchanger
37,39,45 ... well heater
38 ... the first shift-converter
40 ... transformationreation water vapour
41 ... generation gas after transformationreation
42 ... CO
2absorption tower
43 ... CO
2generation gas after absorption
46 ... CO
2regenerator column
47,48 ... CO
2absorption liquid
49 ... well heater
50 ... CO
2the regeneration heating steam of absorption liquid
52 ... CO
2compressor
53 ... by the generation gas of transformationreation high temperature
54 ... the second shift-converter
55 ... conversion interchanger
56 ... the dry water vapour of using
57 ... flow control valve
58 ... supply steam
60 ... flow control valve
61 ... the gas of oxygen-free gas
62 ... cleaning apparatus
63 ... solids disperses
101 ... reclaim CO
2
102 ... recycling CO
2
103 ... store CO
2
104 ... compression CO
2
GF ... vapourizing furnace
Claims (9)
1. a solid-fuelled gasification system, is characterized in that,
This gasification system possesses: solid-fuelled hopper, fuel carrying loop, vapourizing furnace, generation gas cooling portion, cleaning apparatus, washing tower and desulfurizer after drying installation dry solid fuel, dried solid-fuelled shredding unit, storage are pulverized, the gas that contains water vapour that will produce at described drying installation mix with the generation gas that comes from described vapourizing furnace in the downstream side of described vapourizing furnace.
2. solid-fuelled gasification system according to claim 1, is characterized in that,
This gasification system possesses: CO shift-converter and CO
2recovering mechanism, described hopper has locking hopper and hopper, and the gas that contains water vapour being produced by described drying installation is supplied with at least one party in described generation gas cooling portion and described CO shift-converter.
3. solid-fuelled gasification system according to claim 2, is characterized in that,
This gasification system possesses the generation gas supply circuit that the generation gas that comes from described CO shift-converter is supplied with to described drying installation, and the reaction heat of described CO shift-converter is used as to the drying source in described drying installation.
4. solid-fuelled gasification system according to claim 2, is characterized in that,
This gasification system possesses the water vapour supply circuit that is arranged on the heat recovery section in described CO shift-converter downstream and the water vapour being produced by this heat recovery section is supplied with to described drying installation, and the reaction heat in CO shift-converter is used as to the drying source in described drying installation.
5. solid-fuelled gasification system according to claim 2, is characterized in that,
Described CO
2recovering mechanism has CO
2regenerator column, this CO
2regenerator column possesses described CO
2the regeneration heating part that a part for absorption liquid heats, this gasification system possesses water vapour feed mechanism, and this water vapour feed mechanism possesses and will heat described CO by described regeneration heating part
2the water vapour supply circuit that water vapour after absorption liquid is supplied with to described drying installation, and will be by described regeneration heating part heating CO
2water vapour after absorption liquid is as the drying source in described drying installation.
6. solid-fuelled gasification system according to claim 2, is characterized in that,
This gasification system possesses compression CO
2sensible heat as the feed mechanism of described solid-fuelled drying source, this feed mechanism possesses compression set and CO
2supply circuit, described compression set will be by described CO
2the CO that recovering mechanism reclaims
2compression, described CO
2supply circuit will compress CO
2supply with to described drying installation.
7. solid-fuelled gasification system according to claim 6, is characterized in that,
This gasification system possesses compression CO
2to described drying installation supply and as described solid-fuelled drying source, by described compression CO
2the supply circuit of supplying with to described locking hopper and described hopper, by described compression CO
2as lead to being dried of described vapourizing furnace solid-fuelled transporting medium.
8. solid-fuelled gasification system according to claim 6, is characterized in that,
This gasification system possesses described compression CO
2sensible heat as the feed mechanism of described solid-fuelled drying source and dried solid-fuelled preheating, this feed mechanism possesses compression CO
2the CO supplying with to described drying installation, described locking hopper and described hopper respectively
2supply circuit.
9. solid-fuelled gasification system according to claim 8, is characterized in that,
The gas that contains water vapour being produced by described locking hopper and described hopper is mixed with the generation gas that comes from this vapourizing furnace in the downstream side of described vapourizing furnace.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
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| JP2012246021A JP6057674B2 (en) | 2012-11-08 | 2012-11-08 | Gasification system for high moisture solid fuel |
| JP2012-246021 | 2012-11-08 |
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| CN103805280A true CN103805280A (en) | 2014-05-21 |
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| CN105571303A (en) * | 2016-01-27 | 2016-05-11 | 北京神雾环境能源科技集团股份有限公司 | System and method for treating low-rank coals |
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| JP6231842B2 (en) * | 2013-10-08 | 2017-11-15 | 三菱日立パワーシステムズ株式会社 | Gasification system with gasification furnace |
| JP6938146B2 (en) * | 2016-12-14 | 2021-09-22 | 三菱パワー株式会社 | Gasifier equipment and its operation method |
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| AU2013251229A1 (en) | 2014-05-22 |
| JP2014095004A (en) | 2014-05-22 |
| JP6057674B2 (en) | 2017-01-11 |
| AU2013251229B2 (en) | 2016-04-21 |
| CN103805280B (en) | 2017-04-12 |
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