CN103409152A - Technology and system for upgrading low-rank coal through high-heating-value gas heat carrier - Google Patents
Technology and system for upgrading low-rank coal through high-heating-value gas heat carrier Download PDFInfo
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- CN103409152A CN103409152A CN201310318269XA CN201310318269A CN103409152A CN 103409152 A CN103409152 A CN 103409152A CN 201310318269X A CN201310318269X A CN 201310318269XA CN 201310318269 A CN201310318269 A CN 201310318269A CN 103409152 A CN103409152 A CN 103409152A
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Abstract
The invention discloses a technology and a system for upgrading low-rank coal through a high-heating-value gas heat carrier, and solves the problems that the conventional technology for upgrading low-rank coal through the high-heating-value gas heat carrier cannot directly utilize a great amount of low-heat-value pyrolysis gas, and the operation cost is high. The technical scheme comprises the following steps: conveying raw coal to a drying furnace for drying; then conveying the raw coal to a pyrolysis furnace for pyrolysis; obtaining semicoke and crude pyrolysis gas after water and most volatile components are removed; performing dust removing, washing and cooling on the crude pyrolysis gas, wherein the pyrolysis gas subjected to dust removing, washing and cooling can be divided into at least two parts, the first part of pyrolysis gas is conveyed to the pyrolysis heating furnace as fuel, the generated high-temperature fume is used for indirectly heating the second part of pyrolysis gas which is conveyed to the pyrolysis heating furnace, and the heated pyrolysis gas is conveyed to the pyrolysis furnace to supply heat for the pyrolytic reaction of the dried raw coal. The technology is simple, high in operation stability of system, low in cost and environment-friendly, and can generate pyrolysis gas which is high in heating value and can be completely recycled by the system.
Description
Technical field
The present invention relates to a kind of low-rank coal process for upgrading and system, specifically a kind of high heat value gas thermal barrier low-rank coal process for upgrading and system.
Background technology
The research of low-rank coal upgrading technology starts from 20th century the eighties, and through the development of nearly 40 years, it is ripe that part low-rank coal upgrading technology has been tending towards, and progressively be applied in suitability for industrialized production.According to low-rank coal upgrading degree, divide, low-rank coal upgrading technology mainly is divided into drying (moulding) the dehydration upgrading technology of Physical and pyrolysis (destructive distillation) the upgrading technology two large classes of chemical method both at home and abroad at present.
Low order improving quality of coal by pyrolysis technology ultimate principle is that low-rank coal is under isolated air (or at nonoxidizing atmosphere) condition, pyrolytic reaction and pyrogenic reaction occur in (350～800 ℃) at higher temperature, are removing moisture and most of volatile and are generating the process of coal gas, tar and semicoke.In pyrolysis upgrading process, the chemical transformation such as coking and thermolysis have occurred in the low-rank coal coal body.This technology, according to the heating medium difference, is divided into gaseous heat-carrier pyrolytic technique and solid heat carrier pyrolysis technology.The gaseous heat-carrier pyrolytic technique is by being used hot gas, as thermal source, the low-rank coal coal is carried out to pyrolysis; The solid thermal carriers technology is to use hot solids to mix with brown coal as thermal source (high temperature semicoke or porcelain ball etc.), utilizes the sensible heat of solid thermal carriers brown coal to be heated to a kind of process for upgrading of pyrolysis.
The relative solid thermal carriers technique of gaseous heat-carrier pyrolytic process, operational condition relax easily control, and the pyrolytic process oil offtake is large, the tar quality better obtained.But because adopting high-temperature flue gas usually, traditional gaseous heat-carrier pyrolytic process with brown coal, directly contacts CO, H that the pyrolysis of coal process produces as thermal barrier
2With the combustibleconstituents such as hydro carbons, diluted by a large amount of heated air, thereby the pyrolysis gas calorific value obtained is very low, generally is about 300～500 kcal/Nm
3, this technological process exists a large amount of low heat value pyrolysis gas to be difficult to the problem that directly burning utilizes, and must a large amount of high heating value burning gas of blending (as Sweet natural gas) could burn, and greatly has influence on running cost.
Summary of the invention
To the objective of the invention is in order solving the problems of the technologies described above, to provide that a kind of technique is simple, serviceability is high, cost is low, environmentally friendly, the high and high heat value gas thermal barrier low-rank coal process for upgrading all native system reuses of the pyrolysis gas calorific value of generation.
The present invention also provides a kind of thermal barrier of high heat value gas for above-mentioned technique low-rank coal upgrading system.
High heat value gas thermal barrier low-rank coal process for upgrading of the present invention is: raw coal is entered to the pyrolysis oven pyrolysis after sending into kiln dried, after having removed residual moisture and most of volatile, obtain semicoke and thick pyrolysis gas, described thick pyrolysis gas carries out dedusting, the washing cooling, it is characterized in that, described dedusting, pyrolysis gas after the washing cooling is divided into two portions at least, first part's pyrolysis gas is sent into the pyrolysis heater burning that acts as a fuel, the high-temperature flue gas produced carries out indirect heating to the second section pyrolysis gas of sending into pyrolysis heater, pyrolysis gas after heating is delivered to pyrolysis oven and is provided thermal source for the pyrolytic reaction of dried raw coal.
Described pyrolysis gas is divided into three parts, and wherein, the third part pyrolysis gas is sent into dry Coalhotairfurnace fuel and coal dust mixed firing as a supplement, after the flue gas ash removal of generation, sends into dry raw coal in drying oven.
Flue gas after institute's pyrolysis heater heat exchange is sent into dry Coalhotairfurnace and is mixed with described flue gas.
The dry cryodrying gas dedusting rear section produced of described raw coal is recycled to dry Coalhotairfurnace mixes with high-temperature flue gas, and rest part effluxes.
After isolated coal dust in cryodrying gas and the coal dust that separates in thick pyrolysis gas merge, send into after Pulverized Coal Bin is stored and be sent to dry Coalhotairfurnace and act as a fuel.
The dedusting of the thick pyrolysis gas after described pyrolysis oven pyrolysis, washing cool-down method are: thick pyrolysis gas is first through the tornado dust collector dedusting, then washs cooling through reverse contact of quenching column and coal tar, finally by the further decoking of electrical tar precipitator.
A kind of thermal barrier of high heat value gas for above-mentioned technique low-rank coal upgrading system, comprise the drying oven and the pyrolysis oven that through pipeline, connect successively, the pneumatic outlet of described pyrolysis oven connects pyrolysis tornado dust collector, quenching column, electrical tar precipitator and pyrolysis recirculation blower successively, the outlet of described pyrolysis recirculation blower is connected with fuel inlet and the pyrolysis gas entrance of pyrolysis heater respectively, and the pyrolysis gas outlet of described pyrolysis heater is connected with the pyrolysis gas import of pyrolysis oven.
The outlet of described pyrolysis recirculation blower also is connected with the fuel inlet of dry Coalhotairfurnace, the exhanst gas outlet of described pyrolysis heater is connected with the smoke inlet of dry Coalhotairfurnace, and the exhanst gas outlet drying flue gas tornado dust collector of described dry Coalhotairfurnace are connected with the smoke inlet of drying oven.
The dry gas outlet drying sack cleaner of described drying oven, dry recycle blower fan are connected with the smoke inlet of dry Coalhotairfurnace.
The discharge of the discharge of described pyrolysis tornado dust collector and dry flue gas tornado dust collector all is connected with the Pulverized Coal Bin entrance through separately screw feeder, and described Pulverized Coal Bin outlet is connected with the fuel inlet of dry Coalhotairfurnace.
Described first part pyrolysis gas accounts for 5～20% of total pyro lysis temperature tolerance volume, and the second section pyrolysis gas accounts for 60～95% of total pyro lysis temperature tolerance, and remainder is the third part pyrolysis gas.
Technical process of the present invention adopts the pyrolysis gas of high heating value, as the pyrolysis thermal barrier, dried raw coal is carried out to pyrolysis, thereby can guarantee out that the pyrolysis gas calorific value of pyrolysis oven is higher, reaches 2000 Kcal/Nm
3Above, thus subsequent technique can directly utilize this gas, and without filling into again the fuel such as Sweet natural gas.The pyrolysis gas part cyclically utilizing of acquisition is carried out to pyrolysis to raw coal, part acts as a fuel and sends into pyrolysis heater the pyrolysis gas of reuse is carried out to indirect heating, avoid flue gas to sneak in the pyrolysis gas of reuse, remaining part can also be sent into dry Coalhotairfurnace fuel generation high-temperature flue gas as a supplement, thereby realizes whole system self-energy self-equilibrating; In addition, the coal dust reclaimed in dust removal process also can be sent into the burning that acts as a fuel of dry Coalhotairfurnace, and the energy produced in whole pyrolytic process is fully used, and does not need, from external complement fuel, greatly to have reduced the running cost of whole system fully.
Further, in quenching column, adopt coal tar to carry out dedusting, cooling and absorption to pyrolysis gas, utilize the similar principle that mixes to reclaim the coal tar component in pyrolysis gas, the recycling electrical tar precipitator carries out secondary and catches Jiao, can be effectively by the coal tar recovering in pyrolysis gas, in the pyrolysis gas after processing, coal tar content is less than 1ppmv.And adopt coal tar as cooling, washing medium, and do not consume fresh water, to after the pyrolysis gas wash cooling, not producing waste water, do not cause environmental pollution yet, and can also obtain high-quality coal-tar products, be specially adapted to the purification of the pyrolysis gas that coal tar content is high.
Technique of the present invention is simple, the system reform and running cost is low, capacity usage ratio is high, can realize whole system self-energy self-equilibrating, without outer for fuel, can produce the pyrolysis gas of high heating value (at 2000Kcal/Nm
3Above), without waste water produce, the waste gas generation is few, can significantly reduce the running cost, environmentally friendly of system.
The accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention and system diagram.
Wherein, 1-pyrolysis heater, 2-pyrolysis oven, 3-pyrolysis tornado dust collector, 4-quenching column, 5-PCT recycle pump, 6-PCT water cooler, 7-electrical tar precipitator, 8-pyrolysis recirculation blower, 9-dry Coalhotairfurnace, 10-drying oven, 11-dry sack cleaner, 12-dry recycle blower fan, 13-Quench dish, 14-screw feeder, 15-screw feeder, 16-dry flue gas tornado dust collector, 17-Pulverized Coal Bin.
Embodiment
System embodiment:
With reference to Fig. 1, drying oven 10, pyrolysis oven 2 and Quench dish 13 are connected successively, the pneumatic outlet of described pyrolysis oven 2 connects pyrolysis tornado dust collector 3, quenching column 4, electrical tar precipitator 7 and pyrolysis recirculation blower 8 successively, the outlet of described pyrolysis recirculation blower 8 is connected with the fuel inlet of pyrolysis heater 1 and the smoke inlet of pyrolysis gas entrance and dry Coalhotairfurnace respectively, and the pyrolysis gas outlet of described pyrolysis heater 1 is connected with the pyrolysis gas import of pyrolysis oven 2.
The exhanst gas outlet of described pyrolysis heater 1 is connected with the flue gas admission port of dry Coalhotairfurnace 9, and the exhanst gas outlet drying flue gas tornado dust collector 16 of described dry Coalhotairfurnace 9 are connected with the smoke inlet of drying oven 10.The dry gas outlet drying sack cleaner 11 of described drying oven 10, dry recycle blower fan 12 are connected with the smoke inlet of dry Coalhotairfurnace 9.
The discharge of the discharge of described pyrolysis tornado dust collector 3 and dry flue gas tornado dust collector 11 all is connected with Pulverized Coal Bin 17 entrances through separately screw feeder 14,15, and described Pulverized Coal Bin 17 outlets are connected with the fuel inlet of dry Coalhotairfurnace 9.
The coal tar outlet of described quenching column 4 bottoms is connected with the coal tar import at quenching column 4 tops through PCT recycle pump 5, PCT water cooler 6.
Process example:
With reference to Fig. 1, flue gas drying to the water content that raw coal is sent into temperature in the interior quilt of drying oven 10 is weight percentage 20～40%, obtain cryodrying gas (temperature is 100～150 ℃) and dried raw coal, described dried then sending in pyrolysis oven 2 carried out pyrolysis, the semicoke obtained and pyrolysis gas, described semicoke is transmitting system after the 13 Quench coolings of Quench dish; the pyrolysis gas obtained (360～420 ℃) is sent into quenching column 4 again after pyrolysis tornado dust collector 3 are isolated coal dust, the reverse tar composition directly contacted in the washing pyrolysis gas of coal tar (PCT) come with the tower top circulation in quenching column 4, in pyrolysis gas after dedusting washing cooling, coal tar content is less than 1ppmv, the pyrolysis gas temperature of controlling out quenching column 4 enters electrical tar precipitator 7 at least in its dew-point temperature more than 10 ℃, after electrical tar precipitator 7 is processed pyrolysis gas in (coal tar content is less than 1ppmv, dustiness is less than 1ppmv) after carrying, pyrolysis recirculation blower 8 is divided into three parts, first part's (accounting for the volume percent 5～20% of pyrolysis gas total amount) pyrolysis gas is sent into pyrolysis heater 1 and is acted as a fuel, the high-temperature flue gas produced carries out indirect heating to the second section pyrolysis gas (accounting for the volume percent 60～95% of pyrolysis gas total amount) of sending into pyrolysis heater 1, pyrolysis gas after heating (temperature is 550～600 ℃) is delivered to pyrolysis oven 2 and is directly contacted with dried raw coal as carrier gas, for the pyrolytic reaction of raw coal provides thermal source, third part pyrolysis gas (account for circulation gas total amount 0～20%) is sent into dry Coalhotairfurnace 9 fuel and coal dust mixed firing as a supplement, after flue gas (260～320 ℃) dedusting of temperature, sends into dry raw coal in drying oven 1 in generation.Flue gas after the interior heat exchange of pyrolysis heater 1 is sent into dry Coalhotairfurnace 9.The cryodrying gas drying sack cleaner 11 that described moisture eliminator 10 is discharged is isolated after coal dust drying recirculation blower 12 parts again and is effluxed (going desulphurization system), part is recycled to dry Coalhotairfurnace 9, the exhaust gas volumn properly distributed that described outer discharge capacity can be required according to dry raw coal.Described dry sack cleaner 11 and the isolated coal dust of dry sack cleaner 11 can partly efflux (going the pulverized coal forming system), and part is recycled to after Pulverized Coal Bin 17 is collected sends into dry Coalhotairfurnace 9 for making fuel combustion generation flue gas.Described outer discharge capacity can be according to the required coal dust amount properly distributed of dry Coalhotairfurnace 9 burning.
The low-rank coal upgrading system of producing 1000000 tons per year of take is example, and the pyrolysis gas calorific value obtained after pyrolysis can reach 2000kcal/Nm
3, can save 1.2 ten thousand tons of gas consumptions every year, reclaim 50,000 tons, coal tar.
Claims (10)
1. high heat value gas thermal barrier low-rank coal process for upgrading, raw coal is entered to the pyrolysis oven pyrolysis after sending into kiln dried, after having removed residual moisture and most of volatile, obtain semicoke and thick pyrolysis gas, described thick pyrolysis gas carries out dedusting, the washing cooling, it is characterized in that, described dedusting, pyrolysis gas after the washing cooling is divided into two portions at least, first part's pyrolysis gas is sent into the pyrolysis heater burning that acts as a fuel, the high-temperature flue gas produced carries out indirect heating to the second section pyrolysis gas of sending into pyrolysis heater, pyrolysis gas after heating is delivered to pyrolysis oven and is provided thermal source for the pyrolytic reaction of dried raw coal.
2. high heat value gas thermal barrier low-rank coal process for upgrading as claimed in claim 1, it is characterized in that, described pyrolysis gas is divided into three parts, wherein, the third part pyrolysis gas is sent into dry Coalhotairfurnace fuel and coal dust mixed firing as a supplement, after the flue gas ash removal of generation, sends into dry raw coal in drying oven.
3. high heat value gas thermal barrier low-rank coal process for upgrading as claimed in claim 1 or 2, is characterized in that, the flue gas after institute's pyrolysis heater heat exchange is sent into dry Coalhotairfurnace and mixed with described high-temperature flue gas.
4. high heat value gas thermal barrier low-rank coal process for upgrading as claimed in claim 1 or 2, is characterized in that, the dry cryodrying gas dedusting rear section produced of described raw coal is recycled to dry Coalhotairfurnace mixes with flue gas, and rest part effluxes.
5. high heat value gas thermal barrier low-rank coal process for upgrading as claimed in claim 4, it is characterized in that, after isolated coal dust in cryodrying gas and the coal dust that separates in thick pyrolysis gas merge, send into after Pulverized Coal Bin is stored and be sent to dry Coalhotairfurnace and act as a fuel.
6. high heat value gas thermal barrier low-rank coal process for upgrading as claimed in claim 1, it is characterized in that, the dedusting of the thick pyrolysis gas after described pyrolysis oven pyrolysis, washing cool-down method are: thick pyrolysis gas is first through the tornado dust collector dedusting, through reverse contact of quenching column and coal tar, wash cooling again, finally by the further decoking of electrical tar precipitator.
7. the low-rank coal of the high heat value gas thermal barrier for the described technique of claim 1-6 any one upgrading system, comprise the drying oven and the pyrolysis oven that through pipeline, connect successively, the pneumatic outlet of described pyrolysis oven connects pyrolysis tornado dust collector, quenching column, electrical tar precipitator and pyrolysis recirculation blower successively, it is characterized in that, the outlet of described pyrolysis recirculation blower is connected with fuel inlet and the pyrolysis gas entrance of pyrolysis heater respectively, and the pyrolysis gas outlet of described pyrolysis heater is connected with the pyrolysis gas import of pyrolysis oven.
8. high heat value gas thermal barrier low-rank coal upgrading system as claimed in claim 7, it is characterized in that, the outlet of described pyrolysis recirculation blower also is connected with the fuel inlet of dry Coalhotairfurnace, the exhanst gas outlet of described pyrolysis heater is connected with the smoke inlet of dry Coalhotairfurnace, and the exhanst gas outlet drying flue gas tornado dust collector of described dry Coalhotairfurnace are connected with the smoke inlet of drying oven.
9. high heat value gas thermal barrier low-rank coal upgrading system as claimed in claim 8, is characterized in that, the dry gas outlet drying sack cleaner of described drying oven, dry recycle blower fan are connected with the smoke inlet of dry Coalhotairfurnace.
10. as the described high heat value gas thermal barrier of claim 7-9 any one low-rank coal upgrading system, it is characterized in that, the discharge of the discharge of described pyrolysis tornado dust collector and dry flue gas tornado dust collector all is connected with the Pulverized Coal Bin entrance through separately screw feeder, and described Pulverized Coal Bin outlet is connected with the fuel inlet of dry Coalhotairfurnace.
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Cited By (7)
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| CN103756698A (en) * | 2014-01-22 | 2014-04-30 | 鞍山兴德工程技术有限公司 | Low-grade coal gas flow injection dense-phase quick dry distillation upgrading method and system |
| CN104610990A (en) * | 2015-01-14 | 2015-05-13 | 太原理工大学 | Low-rank coal adiabatic pyrolysis device |
| CN106833696A (en) * | 2017-01-23 | 2017-06-13 | 武汉光谷蓝焰新能源股份有限公司 | A kind of biomass pyrolytic polygenerations systeme |
| CN106916598A (en) * | 2017-03-23 | 2017-07-04 | 肖国雄 | A kind of interrupted pyrolysis oven of destructive distillation type tunnel type |
| CN107118785A (en) * | 2017-04-21 | 2017-09-01 | 太原理工大学 | The self-heating spontaneous combustion process energy utilization method of low-order coal |
| CN110564437A (en) * | 2019-09-18 | 2019-12-13 | 中国科学院山西煤炭化学研究所 | system and method for improving quality of coal in front of pulverized coal furnace |
| CN112852459A (en) * | 2020-12-24 | 2021-05-28 | 陕西煤业化工集团神木天元化工有限公司 | Pulverized coal pyrolysis device and pyrolysis method |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103756698A (en) * | 2014-01-22 | 2014-04-30 | 鞍山兴德工程技术有限公司 | Low-grade coal gas flow injection dense-phase quick dry distillation upgrading method and system |
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| CN106833696A (en) * | 2017-01-23 | 2017-06-13 | 武汉光谷蓝焰新能源股份有限公司 | A kind of biomass pyrolytic polygenerations systeme |
| CN106916598A (en) * | 2017-03-23 | 2017-07-04 | 肖国雄 | A kind of interrupted pyrolysis oven of destructive distillation type tunnel type |
| CN106916598B (en) * | 2017-03-23 | 2020-06-26 | 肖国雄 | Dry distillation type tunnel type intermittent pyrolysis furnace |
| CN107118785A (en) * | 2017-04-21 | 2017-09-01 | 太原理工大学 | The self-heating spontaneous combustion process energy utilization method of low-order coal |
| CN110564437A (en) * | 2019-09-18 | 2019-12-13 | 中国科学院山西煤炭化学研究所 | system and method for improving quality of coal in front of pulverized coal furnace |
| CN110564437B (en) * | 2019-09-18 | 2021-02-09 | 中国科学院山西煤炭化学研究所 | System and method for improving quality of coal in front of pulverized coal furnace |
| CN112852459A (en) * | 2020-12-24 | 2021-05-28 | 陕西煤业化工集团神木天元化工有限公司 | Pulverized coal pyrolysis device and pyrolysis method |
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Application publication date: 20131127 |