CN104073298A - Device and method for reducing content of ash in lignite gasification synthesis gas - Google Patents
Device and method for reducing content of ash in lignite gasification synthesis gas Download PDFInfo
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- CN104073298A CN104073298A CN201410307145.6A CN201410307145A CN104073298A CN 104073298 A CN104073298 A CN 104073298A CN 201410307145 A CN201410307145 A CN 201410307145A CN 104073298 A CN104073298 A CN 104073298A
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- 239000003077 lignite Substances 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 19
- 230000015572 biosynthetic process Effects 0.000 title abstract description 6
- 238000003786 synthesis reaction Methods 0.000 title abstract description 6
- 238000002309 gasification Methods 0.000 title abstract 3
- 239000002245 particle Substances 0.000 claims abstract description 52
- 230000009467 reduction Effects 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 123
- 239000000843 powder Substances 0.000 claims description 16
- 239000002002 slurry Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- 239000004744 fabric Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 4
- 239000006052 feed supplement Substances 0.000 claims description 4
- 235000012054 meals Nutrition 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 235000019362 perlite Nutrition 0.000 claims description 3
- 239000010451 perlite Substances 0.000 claims description 3
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 239000000463 material Substances 0.000 claims 1
- 239000000428 dust Substances 0.000 abstract description 41
- 238000000746 purification Methods 0.000 abstract description 7
- 230000009347 mechanical transmission Effects 0.000 abstract 1
- 230000003068 static effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 15
- 238000001914 filtration Methods 0.000 description 6
- 239000003245 coal Substances 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000002688 persistence Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
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Abstract
The invention provides a device and a method for reducing the content of ash in lignite gasification synthesis gas. The main contents of the method are as follows: dust-containing high-temperature synthesis gas generated during lignite gasification passes through two or more intermittent motion bed layers, and the majority of dust can be interrupted by the intermittent motion bed layers, thus realizing the purification of the synthesis gas. Under the operating state of the device, particles in the bed layers keep static so as to maintain high dust removal efficiency, a great amount of dust can be accumulated in the bed layers after the device runs for certain time, to cause the reduction of the dust removal efficiency, the particles containing dust are moved out of the bed layers by virtue of a control valve, and meanwhile dustless particles are supplemented to complete the ash removal treatment, thus recovering the dust removal efficiency. The device is simple in structure, convenient to operate, easy in control over gas pressure and flow, and free from mechanical transmission. The method is a reliable and portable means for dust removal of the high-temperature synthesis gas.
Description
Technical field
The present invention relates to technical field of coal chemical industry, especially relate to a kind of apparatus and method that reduce ash oontent in brown coal hydrogasification synthetic gas
Background technology
At present, many countries high-temperature dust removal technology in research Filter Tuber For Clean Coal combustion technology all in the world, wherein high-temperature synthesis gas dedusting is the important procedure in coal power generation and Coal Chemical Industry industry.The degree of purification of synthetic gas is not only related to the safe operation of internal combustion turbine, and is the requirement that meets the environmental law Laws & Regulations of increasingly stringent.
At present, generally believe in the world: can take into account efficiency and continuously the dust collecting process of operating performance be the technology being hopeful most with development prospect.Main high-temperature dust removal technology mainly comprises now: cyclone dust collection technology, high temperature electrostatic trapping dedusting technology, ceramic filter dedusting technology, metal felt dust removal by filtration technology, moving granular bed dust removal by filtration technology etc.These technology are all in the research and development stage, and dust removal mechanism and efficiency of dust collection respectively have feature.For example: cyclone dust collection technology is to utilize centrifugal action by dust separation and collection from air-flow, but efficiency of dust collection is only 85% left and right, can only the larger dust of particle separation diameter; High temperature electrostatic dedusting is to utilize high-voltage power supply and pair of electrodes to produce inhomogeneous electric field with the dust in separation and collection air-flow, the efficiency of electric precipitation reaches 95%, but one-time investment and working cost are very high, also there is the problems such as the susceptibility of the character such as the ratio resistance of dust and gaseous constituent and electrode corrosion; Ceramic filter efficiency of dust collection is high, reaches more than 99%, can remove grits more than 5 μ m, can be high temperature resistant, but exist sealing problem, the permanent obstruction of filtering membrane hole and pressure drop to continue increase problem etc., affect reliability and weather resistance; Metal felt filters and can carry out meticulous dedusting to the grit below 5 μ m, and under normal temperature, long term operation better but have the not corrosion resistant problem of non-refractory.
Along with the development of dedusting technology under High Temperature High Pressure, to the simplification of dust removal installation, high temperature, high efficiency, require increasingly strong.Moving granular bed dust removal by filtration generally believes in the world and substantially can realize efficiency and one of the most promising technology of operating performance continuously taken into account.
Summary of the invention
The problem that the invention will solve be to provide a kind of reduce brown coal hydrogasification synthetic gas ash oontent apparatus and method.This device has following characteristics: simple in structure, easy to operate, persistence is good, efficiency of dust collection is high, cost is low, duration of service is long, high temperature resistant, gaseous tension and flow are easily controlled and do not need mechanical rotation, can at high temperature operate, reliably convenient.
For solving the problems of the technologies described above, the technical scheme that the invention adopts is: a kind of device that reduces ash oontent in brown coal hydrogasification synthetic gas, comprise gas wash tower, ash disposal system and remove ash gas source of the gas, in described gas wash tower, be provided with the intermittent movement bed of several inclinations, in intermittent movement bed, be filled with movably particle; Describedly be connected by riser tube with ash disposal system except ash gas source of the gas, described intermittent movement bed and riser tube, be all connected by pipeline between ash disposal system and intermittent movement bed, and connected pipeline is equipped with ball valve, and preferably, ball valve is V-type ball valve.Because V-type ball valve can not destroy the wear-resistant medium particle in bed when regulating, most dust is tackled by the particle on intermittent movement bed, plays the effect of decontaminating syngas.
Further, the quantity of described intermittent movement bed is two or more, can remove more up hill and dale dust like this, and intermittent movement bed is inclined, for below except the ash of degranulation absorption step by step in, the particle flow in intermittent movement bed is convenient.
Further; described ash disposal system comprises particle surge tank, expands slurry tank, cyclonic separator, fine powder cloth bag collector; particle surge tank is communicated with expansion slurry tank; cyclonic separator is positioned at and expands slurry tank inside; fine powder cloth bag collector is positioned at the outside that expands slurry tank; and be communicated with cyclonic separator, fine powder cloth bag collector is provided with deashing tail gas discharging pipe.
Further, the sidewall of described particle surge tank is provided with feed supplement tank.
Further, described particle is perlite, sandstone, and pottery, a kind of in silicon oxide, and particle is ball-type, diameter is 0.5～1.0mm.The less filtration efficiency of particle is better in theory, but particle diameter is less than after 0.5mm, will cause the pressure drop between bed excessive, and after being greater than 1.0mm, cake layer is difficult to form, and to the filtration efficiency of dust granules, will reduce a lot.
Further, in described intermittent movement bed, bed height is 20～500mm, in order to improve efficiency of dust collection and to maintain acceptable bed pressure drop.
The invention also discloses a kind of method of using the device of ash oontent in reduction brown coal hydrogasification synthetic gas as above, comprise the steps:
1), the synthetic gas after brown coal hydrogasification is passed in tower from the top of gas wash tower, synthetic gas is successively by several intermittent movement beds, and under the endocorpuscular effect of intermittent movement bed, most of ash content is blocked;
2), when intermittent movement bed is used after 15 days～90 days; on intermittent movement bed, can accumulate a large amount of ash contents; now; need to carry out ash disposal processing to intermittent movement bed: in ash disposal system operational process; open the two ends ball valve of a certain intermittent movement bed; the ash content of particle and absorption is because Gravitational sliding is to riser tube; then by gas, deliver into and expand in slurry tank; particle, because action of gravity and ash separation drop to particle surge tank, then slides to down intermittent movement bed and carries out recycle.
3), by step 2) in the two ends ball valve of the intermittent movement bed opened close, then open all the other certain intersegmental mobile bed two ends ball valves of having a rest, repeat above-mentioned steps and carry out deashing.
Preferably, step 2) in, when ash disposal system is moved, the fine powder after cyclonic separator separation carries and through cyclonic separator separation, enters in fine powder cloth bag collector and collect down at deashing gas, clean except ash gas emptying or collect recycling through ash disposal tail gas discharging pipe; Through the meal of cyclonic separator separation, through the dipleg position of cyclonic separator, discharge and be collected into meal cloth bag collector, clean except ash gas is emptying or collect recycling.
Preferably, described except ash gas source of the gas be synthetic gas or the rare gas element after dedusting.
Preferably, the synthetic gas after selecting dedusting is as source of the gas, and the synthetic gas after described dedusting is ash disposal collection and confinement of gases recycling; When selecting rare gas element as source of the gas, preferred nitrogen, preferably the ash gas that removes of cleaning is discharged mode.
Advantage and positively effect that the invention has are: simple in structure, easy to operate, persistence is good, efficiency of dust collection is high, cost is low, duration of service is long, high temperature resistant, gaseous tension and flow are easily controlled and do not need mechanical rotation, can at high temperature to synthetic gas, carry out ash disposal.Device in the present invention, dust removal efficiency reaches 99.0%-99.9%, removes the particle diameter of dust at 2 μ m-20 μ m, the 50-200m of the synthetic gas that cleaning apparatus is processed
3/ h, the concentration of the outlet ash content of the synthetic gas after purification is 4-30mg/m
3.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation that reduces the device of ash oontent in brown coal hydrogasification synthetic gas;
In figure: 1, gas wash tower; 2, particle surge tank; 3, expand slurry tank; 4, cyclonic separator; 5, fine powder cloth bag collector; 6, except ash gas source of the gas; 7, ball valve; 8, intermittent movement bed; 9, riser tube; 10, deashing tail gas discharging pipe; 11, feed supplement pipe.
Embodiment
A kind of device that reduces ash oontent in brown coal hydrogasification synthetic gas, it is characterized in that: comprise gas wash tower 1, ash disposal system (adding empty frame part in figure) and remove ash gas source of the gas 6, in described gas wash tower 1, be provided with the intermittent movement bed 8 of several inclinations, in intermittent movement bed 8, be filled with movably particle; Describedly be connected by riser tube 9 with ash disposal system except ash gas source of the gas 6, described intermittent movement bed 8 and riser tube 9, be all connected by pipeline between ash disposal system and intermittent movement bed 8, and connected pipeline is equipped with ball valve 7, and ball valve 7 is V-type ball valve.Described ash disposal system comprises particle surge tank 2, expands slurry tank 3, cyclonic separator 4, fine powder cloth bag collector 5; particle surge tank 2 is communicated with expansion slurry tank 3; cyclonic separator 4 is positioned at and expands slurry tank 3 inside; fine powder cloth bag collector 5 is positioned at the outside that expands slurry tank 3; and be communicated with cyclonic separator 4, fine powder cloth bag collector 5 is provided with ash disposal tail gas discharging pipe 10.The sidewall of described particle surge tank 2 is provided with feed supplement tank 11.
A method of using the device of ash oontent in reduction brown coal hydrogasification synthetic gas as above, is characterized in that: comprise the steps:
1), the synthetic gas of brown coal hydrogasification is passed in tower from the top of gas wash tower 1, synthetic gas is successively by several intermittent movement beds 8, and under the endocorpuscular effect of intermittent movement bed 8, most of ash content is blocked;
2), when intermittent movement bed 8 is used after 15 days～90 days; on intermittent movement bed 8, can accumulate a large amount of ash contents; now; need to carry out ash disposal processing to intermittent movement bed 8: in ash disposal system operational process; open the two ends ball valve of a certain intermittent movement bed 8; the ash content of particle and absorption is because Gravitational sliding is to riser tube 9; then by gas, deliver into and expand in slurry tank 3; particle, because action of gravity and ash separation drop to particle surge tank, then slides to down intermittent movement bed 8 and carries out recycle.
3), by step 2) in the two ends ball valve of the intermittent movement bed opened close, then open all the other certain intersegmental mobile bed two ends ball valves of having a rest, repeat above-mentioned steps and carry out deashing.
Step 2) in, when ash disposal system is moved, fine powder after cyclonic separator 4 separation is carrying and through cyclonic separator 4 separation, is entering in fine powder cloth bag collector 5 and collect down except ash gas, and clean deashing gas is emptying or collect recycling through deashing tail gas discharging pipe 10; Through the meal of cyclonic separator separation 4, through the dipleg position of cyclonic separator 4, discharge and collect, clean deashing gas is emptying or collect recycling.
Embodiment mono-～embodiment tetra-below, all adopt structure as above.And adopt method as above to reduce ash oontent in brown coal hydrogasification synthetic gas.
Embodiment mono-
Intermittent movement bed 8 is two, and described particle is perlite, and particle diameter spherical and particle is 0.5mm.The height of described intermittent movement bed 8 is 500mm.
And step 2), in, intermittent movement bed 8 was used after 15 days, carried out ash disposal processing, select except ash gas source of the gas be the synthetic gas after dedusting, the synthetic gas after described dedusting is ash disposal collection and confinement of gases recycling.
Dust removal efficiency in the present embodiment reaches 99.5%, removes the particle diameter of dust in 2 μ m left and right, and the flow of the synthetic gas that cleaning apparatus is processed is 100m
3/ h, the concentration of the outlet ash content of the synthetic gas after purification is 6mg/m
3.
Embodiment bis-
Intermittent movement bed 8 is three, and described particle is sandstone, and particle diameter spherical and particle is 0.8mm.The height of described intermittent movement bed 8 is 400mm.
And step 2), in, intermittent movement bed 8 was used after 30 days, carried out ash disposal processing, select except ash gas source of the gas be the synthetic gas after dedusting, the synthetic gas after described dedusting is deashing collection and confinement of gases recycling.
Dust removal efficiency in the present embodiment reaches 99.6%, removes the particle diameter of dust in 15 μ m left and right, and the flow of the synthetic gas that cleaning apparatus is processed is 150m
3/ h, the concentration of the outlet ash content of the synthetic gas after purification is 14mg/m
3.
Embodiment tri-
Intermittent movement bed 8 is four, and described particle is pottery, and the particle diameter of particle is 0.8mm.The height of described intermittent movement bed 8 is 80mm.
And step 2), in, intermittent movement bed 8 was used after 45 days, carried out ash disposal processing, select except ash gas source of the gas be the synthetic gas after dedusting, the synthetic gas after described dedusting is deashing collection and confinement of gases recycling.
Dust removal efficiency in the present embodiment reaches 99.4%, removes the particle diameter of dust in 18 μ m left and right, and the flow of the synthetic gas that cleaning apparatus is processed is 200m
3/ h, the concentration of the outlet ash content of the synthetic gas after purification is 21mg/m
3.
Embodiment tetra-
Intermittent movement bed 8 is five, and described particle is silicon oxide, and the particle diameter of particle is 1.0mm.The height of described intermittent movement bed 8 is 30mm.
And step 2), in, intermittent movement bed 8 was used after 90 days, carried out ash disposal processing, select except ash gas source of the gas be the synthetic gas after dedusting, the synthetic gas after described dedusting is deashing collection and confinement of gases recycling.
Dust removal efficiency in the present embodiment reaches 99.4%, removes the particle diameter of dust in 18 μ m left and right, and the flow of the synthetic gas that cleaning apparatus is processed is 200m
3/ h, the concentration of the outlet ash content of the synthetic gas after purification is 28mg/m
3.
Above the embodiment of the invention is had been described in detail, but described content is only the preferred embodiment of the invention, can not be considered to for limiting practical range of the present invention.All equalization variations of doing according to the invention scope and improvement etc., within all should still belonging to this patent covering scope.
Claims (10)
1. a device that reduces ash oontent in brown coal hydrogasification synthetic gas, it is characterized in that: comprise gas wash tower (1), ash disposal system and remove ash gas source of the gas (6), the intermittent movement bed (8) that is provided with several inclinations in described gas wash tower (1), intermittent movement bed is filled with movably particle in (8); The described ash gas source of the gas (6) that removes is connected by riser tube (9) with ash disposal system, described intermittent movement bed (8) and riser tube (9), between ash disposal system and intermittent movement bed (8), all by pipeline, be connected, connected pipeline is equipped with ball valve (7), preferably, ball valve (7) is V-type ball valve.
2. the device of ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 1, is characterized in that: the quantity of described intermittent movement bed (8) is two or more.
3. the device of ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 1 and 2; it is characterized in that: described ash disposal system comprises particle surge tank (2), expands slurry tank (3), cyclonic separator (4), fine powder sack cleaner (5); particle surge tank (2) is communicated with expansion slurry tank (3); cyclonic separator (4) is positioned at and expands slurry tank (3) inside; fine powder cloth bag collector (5) is positioned at the outside that expands slurry tank (3); and be communicated with cyclonic separator (4), fine powder cloth bag collector (5) is provided with ash disposal tail gas discharging pipe (10).
4. the device of ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 3, is characterized in that: the sidewall of described particle surge tank (2) is provided with feed supplement tank (11).
5. according to the device of ash oontent in the reduction brown coal hydrogasification synthetic gas described in claim 1～4 any one, it is characterized in that: the material of described particle is perlite, sandstone, pottery, a kind of in silicon oxide, and particle is ball-type, diameter is 0.5～1.0mm.
6. the device of ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 5, is characterized in that: the height of described intermittent movement bed (8) is 20～500mm.
7. a method for the device of ash oontent in the reduction brown coal hydrogasification synthetic gas of use as described in claim 1～6, is characterized in that: comprise the steps:
1), the synthetic gas of brown coal hydrogasification is passed in tower from the top of gas wash tower (1), synthetic gas is successively by several intermittent movement beds (8), and under the endocorpuscular effect of intermittent movement bed (8), most of ash content is blocked;
2), when intermittent movement bed (8) is used after 15 days～90 days; intermittent movement bed can accumulate a large amount of ash contents on (8); now; need to carry out ash disposal processing to intermittent movement bed (8): in ash disposal system operational process; open the two ends ball valve of a certain intermittent movement bed (8); the ash content of particle and absorption is because Gravitational sliding is to riser tube (9); then by gas, deliver into and expand in slurry tank (3); particle, because action of gravity and ash separation drop to particle surge tank (2), then carries out recycle by intermittent movement bed (8).
3), by step 2) in open the intermittent movement bed (8) of two ends ball valve two ends ball valve close, then open all the other certain intersegmental mobile bed (8) two ends ball valves of having a rest, repeat above-mentioned steps and carry out deashing.
8. the method for ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 7, it is characterized in that: step 2) in, when ash disposal system is moved, fine powder after cyclonic separator (4) separation carries and in cyclonic separator (4) separation enters fine powder cloth bag collector (5), collects down at deashing gas, clean except ash gas emptying or collect recycling through ash disposal tail gas discharging pipe (10); Meal through cyclonic separator separated (4) is discharged and is collected through the dipleg position of cyclonic separator (4), and clean deashing gas is emptying or collect recycling.
9. according to the method for ash oontent in the reduction brown coal hydrogasification synthetic gas described in claim 7 or 8, it is characterized in that: described except ash gas source of the gas be synthetic gas or the rare gas element after dedusting.
10. the method for ash oontent in reduction brown coal hydrogasification synthetic gas according to claim 9, is characterized in that: the synthetic gas after selecting dedusting is as source of the gas, and the synthetic gas after described dedusting is deashing collection and confinement of gases recycling; When selecting rare gas element as source of the gas, preferred nitrogen, preferably the deashing gas of cleaning is discharged mode.
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| Publication number | Publication date |
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| CN104073298B (en) | 2016-08-24 |
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Effective date of registration: 20231221 Address after: 300400 Beijing Tianjin Road, Beichen District, Tianjin Patentee after: CHINA TIANCHEN ENGINEERING Co.,Ltd. Patentee after: TIANJIN TIANCHEN GREEN ENERGY ENGINEERING TECHNOLOGY RESEARCH & DEVELOPMENT Co.,Ltd. Patentee after: China Chemical Equipment Technology Group Co.,Ltd. Address before: No. 1 Jingjin Road, Beichen District, Tianjin City, 300400 Patentee before: CHINA TIANCHEN ENGINEERING Co.,Ltd. Patentee before: TIANJIN TIANCHEN GREEN ENERGY ENGINEERING TECHNOLOGY RESEARCH & DEVELOPMENT Co.,Ltd. |