CA1117049A - Method for heat processing of pulverized brown coal - Google Patents
Method for heat processing of pulverized brown coalInfo
- Publication number
- CA1117049A CA1117049A CA000308624A CA308624A CA1117049A CA 1117049 A CA1117049 A CA 1117049A CA 000308624 A CA000308624 A CA 000308624A CA 308624 A CA308624 A CA 308624A CA 1117049 A CA1117049 A CA 1117049A
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- Canada
- Prior art keywords
- brown coal
- heat carrier
- stage
- gaseous heat
- heating
- 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.)
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Abstract
Abstract of the Disclosure According to the invention pulverized brown coal is processed by heating brown coal in two stages. During the first stage brown coal being processed is heated by a gase-ous heat carrier to a temperature at which thermal decomposi-tion of the brown coal begine. During the second stage the brown coal being processed is heated by the gaseous heat carrier to a temperature at which an intensive thermal decom-position of the brown coal takes place. The stream of the gaseous heat carrier delivered at the second stage of heating is fed with air oxygen and with low-grade products, such as heavy tars and pyrogenic water being sprayed into the gaseous heat carrier.
Air oxygen being fed into the gaseous heat carrier as well as heavy tars and pyrogenic water being sprayed into the same raise the combustion temperature of the solid product being obtained and prevent the necessity of purifying the pyrogenic water before disposal thereof into pools. Power consumption required for carrying out the proposed method is approximately the same as that in conventional methods.
Air oxygen being fed into the gaseous heat carrier as well as heavy tars and pyrogenic water being sprayed into the same raise the combustion temperature of the solid product being obtained and prevent the necessity of purifying the pyrogenic water before disposal thereof into pools. Power consumption required for carrying out the proposed method is approximately the same as that in conventional methods.
Description
- . ~
1~17~
~'rHOD ~OR H~A~ PROC~SSING OF PU~V~RIZ~D
BRO',~ C3A~
The invention relates to methods for the destructive processing o~ solid carbo~-containi~g materials, by breaking down thereof and more specifically, to methods for heat pro-cessing o~ pulverized brown coal~.
~ he invention is o~ particular advantage in energe-tic and chemical industries where it can be used for combined production of hi~h-calorific solid and synthetic liquid fuels as well as other gaseous and liquid producbs whioh are subse-quently processed into technical and chemical raw materials.
Background of bhe Invention There are well known in the art methods for pyrolytic, or heat processing of pulverized solid ~uels by the aid of which both usable products, including solid as well as li~uid products, and loY~-grade products, such as heavy tars and pyr-ogenic water are produced.
on ~ hough the heat o~ combustion of heavy tars, the orderof 8400 k~al/kg, is known to be higher than thab o~ the pro-duct being produced (whose heat of combustion is 6400-6700 kcal/kg), the utilization thereof presents a severe problem.
~his problem derives ~rom the ~act that under normal condi-tions t~r is a sticky viscous substance which is neither too ~luid to be delivered through pipelines nor su~`ficiently solid .. ''~ . , ~, .
to be loaded into and delivered by transporting facilities to the consumer. Consequently, when heavy tar is used as a liquid boiler fuel, it is to be transformed into a liquid by heating, which naturally requires additional capital and operating expenses. Yet here, too, the problem of delivering heavy tars to the consumer stands.
Thus, due to heat processing of fuel, the product whose heat of combustion is 8400 kcal/kg practically cannot be used as fuel.
It is also known that pyrogenic water comprises approxi-mately 4.5% phenols dissolved therein which are usable products.
However, to separate phenols from pyrogenic water, a complicated procedure is to be resorted to, which, again requires considerable capital and operating expenses. In addition, after the separation of phenols from pyrogenic water the latter is to be purified prior to disposal into a water pool.
As a consequence of the fact that world's natural ener-gy resources are running thin, processing of large quantities of low-grade fuels is gaining in importance. Specifically, ever more acute becomes a problem of utilizing heavy tar and pyrogenic water which are low-grade products resulting from heat processing of fuels.
There is known in the art a method for heat processing pulverized brown coal (Inventor's Certificate No. 335267 published in 1972, in Bulletin No. 13 "Discoveries, Inventions, Industrial Designs and Trademarks) comprising a first stage of heating the coal by a gaseous heat carrier in less than one second to a tem-perature of 200-. .
i~l7~
5~0C with subsequent separating of the heat carrier from the coal, a second stage of heating the coal by the gaseous heat carrier in less than one second -to a temperature of 500-800C at which an in-tensive thermal decomposition thereof takes place with the formation of a vapour-and-gas suspension consisting of a solid portion and a vapour-and-gas portion, condensing the vapour-and-gas portion to obtain gas, valuable li~uid products and to separate therefrom low-grade products, such as heavy tars and pyrog~enic water.
'~he re~ization o~ the above method makes it possible to produce along with other usable products also low-grade pro-ducts such as heavy tars and pyrogenic water whose utiliza-tion presents a problem not yet solved.
~ he object of the invention is to provide a method for heat pxocessing of pulverized brown coal, which, with the power input equal to that of the conventional methods ensures the production of a solid product with higher heat combustion.
Another object of the present invention is to provide a method for heat processing of pulverized brown coal, which enables utilization of low-grade products.
One more object of the invention is to provide a method for heat processing pulverized solid ~uel, which makes it possible to realize pyrolytic processing o~ the heavy tar -a product of heat processing o~ brown coal.
Still another object o~ the present invention is to pro-vide a method for processing of pu~verized brown coal, which 7Q~9 ehables utili~ation of org~nic substances dissolved in pyrog-enic v~ater.
Summary of the In~ention ~ hese and o-ther objects are achieved by the pro~ision o~ a method for heat processing of` pulverized brown coal com-prising a first stage of heating the coal by a gaseous heat carrier in less than one second to a temperature of 200-500C
and subsequently separating the spent heat carrier frorn the coal, a second stage o~ heating ~he coal by the gaseous car-rier in less than one second to a tempexature o~ ~00-800C at which temperature an intensive thermal decomposition of the coal takes place with the formation of a vapour-and-gas sus-pension containing a solid portion and a vapour_and-gas por-tion, condensing the vapour-and-gas portion to obtain gas, usable liquid product$ and to separate low-grade products, such as heavy tars and pyrogenic water therefrom, wherein, according to the invention, at the second stage R heating the low-grade products of heat processing of pulverized brown coal are sprayed into the stream of`the gaseous carrier con-taining air oxygen.
It is expedient to supply bhe stream of thc gaseous heat carrier v~ith heavy tar? the oxygen oontent in bhe gaseous car-rier being sufficient for carrying out pyrolybic processing of the heavy tar at predetermined temperatures. Due to pyroly-tic processing of the heavy tar, volatile components are liberat-ed which burn and thereby raise the temperature of ~he gaseous ~ 5 -1~17C~9 heat carrier. In addition, there is formed a solid portion v~hich is a high-calori~ic ~uel.
It is good pxactice to supply the stream of the gaseous heat carrier with pyrogenic water, the gaseous heat carrier being supplied along the stream thereof, first ~ith pyroge-nic water and then with heavy tars, ~his prevents the neces-sity in purifying p~rogenic water prior to disposal thereof into water pools. In addition, organic solvents dissolved in pyrogenic: water can be converted into usable products.
Brie~ Description of the Drawings ~ he above-mentioned and other object o~ this invention will become more apparent-by reference to the following des-cription of an embodiment of the invention taken in conjunc-tion with the accompanying drawing which show~ a diagrammat-ic view of an apparatus for heat processing of pulverized bro~ coal.
Description of the Preferred Embodiment of the Invention ~ ihen realizing the method for heat processing of pulver-ized b~own coal, there is used an apparatus comprizing a chamber 1 adapted ~or the ~irst-stage heating of coal. The apparatus has a hopper 2 communicating with the cha~ber 1 through a turnstile ~eeder 3. A co~nection pipe 4 of a devi-ce ~not shown) ~or feeding ~he gaseous heat carrier t~ngen-tially adaoins the chamber 1. ~o discharge the spent gaseous ~ - 6 -i~7~9 heat carrier, the chamber I is provided with a pipe 5 coa-~ially installed therein and connected with a cyclone (not shown). A chamber 7 adapted ~or the second-stage heating of the ~uel is s~ccesively connected to the chamber I ~hrough a ~eeder 6. Abut-tin~ the cha~ber 7 adapted for the second--stage heating of the coal is a means 8 ~or deli~ering the gaseous heat carrier into ~he chamber 7, the stream of the gaseous heat carrier being supplied with low-grade products.
The means 8 is a pipeline 9 tan~entially adjoining the cham-ber 7 adapted for the second-stage heatin~ of the coal. ~he ~ v.el pipeline 9 is provided with a chamber 10 ~or to be burnt therein a~d -to form stack gas, with chamber II ~or pyrogenic water to be ~ed thereto through sprayers 12, and with a chamber 13 ~or heavy tars to be fed thereto throu~h sprayers 14. '~he chamber 10 incorporates a burner 15 adapted to burn fuel in a mixture with air oxy~en.
To discharge the vapour-and-gas mixture resulting ~rom thermal decomposition of the brown coal, the chamber 7 adap- -ted for the second-stage heating o~ fuel is provided ~ith a pipe 16 coaxially positioned therein and connected with a cyclone (not shown) throu~h a pipeline. Furthermore, the chamber 7 adapted ~or the second-stage heating o~ the brown coal is provided with a turnstile metering device 17 adapted to discharge the obtained solid product ~rom the chamber 7.
According to the invention, the method for heat process-in~ o~ pulverized brown coal is realized as follows.
~17(~49 ~ he pulverized brown coal having the size of prticles below I mm is preheated to a temperature about 110C for dry-ing and is -thereafter fed by the feeder 3 from the hopper 2 into the chamber I adapted for the first-stage heating of the brown c~al. Simultaneously an oxygen-~ree heat carrier in the form o~ stack gas having a temperature o~ no less than 500C
is delivered into t~e chamber I through the connection pipe 4.
~ he heat carrier tangentially enters the chamber I adap-ted for the first-stage heating of the brown coal and draws the particles of the pulverized bxown coal. Under the action o~ centri~ug~al and gravity forces the brown coal particles are thrown towards the wall o~ the chamber and descend in a ~ortex. ~he pulverized brown coal is heated by the heat car-rier to a temperature o~ 200 to 500C. ~he spent gaseous heat carrier cooled down to a temperature about 350C is discharg-ed through the pipe 5 into the cyclone (not shown). A portion of the pulverized brown coal carried away by the heat ca~rier is separated there~rom in a conventional manner.
~ he feeder 6 feeds the brown coal being processed from the chamber I adapted ~or the ~irst stage heating o~ the brown coal into the chamber 7 adapted ~or the second stage heatin~
o~ the brown coal. Concurrently with the coal the gaseous heat carrier is ~ed into the chamber 7 adapted ~or the second--sta~e of heating through the means 8. According to the inven-tion the gaseous heat carrier obtained by burning a fuel, such as gas, and by the ~ormation of stack gas is supplied with low-~117~49 -~rade products. ~his procedure is carried QUt in the follovJ-ing way.
A combustible gas or any other fuel mixed with air oxyg-en is ~ed into a burner 15. Iviore than 50% of the combustible gas is burnt in the chamber 10, thereby forming a gaseous heat carrier containing air oxygen. Since approximately 50%
of combus~ible substance are burn-t in the chamber 10 wherein the heat carrier is ~ormed, the temperature in this chamber reaches about 1200C. It is ~o be noted that the process o~
burning and the temperature in the chamber 10 wherein the heat carrier formation takes place are regulated in a conven-tional manner and by conven~ional means and there~ore should be clear to those skilled in the art. From the chamber 10 wherein the heat carrier formation takes place, the gaseous heat carrier enters the chamber II adapted for processing pyrogenetic water. Simultaneously the stream of ~he gaseous heat carrier is supplied with pyrogenic water through the sprayers 12. In the chamber II adapted for processing pyrog-enic water, there takes place evaporation of the water as well as oxidati~e pyrolysis of organic substances dissolved therein, in particular, phenols. On pyrolysis of or~anic substances, one portion thereof gets transformed, another portion burns, still another is deposited as carbon on pulve-rized particles of the obtained coke. Due to processing of the pyrogenic water, the temperature of the gaseous heat car-rier drops to about 1000C. ~he gaseous heat carrier having _ 9 _ ~17Q~9 the tem~erature of 1000C is fed into the chamber 13 where processing of heavy tars takes place~ The chamber 13 is con-tinuously supplied through the sprayers 14 with heav~ tars which constitute a liquid after being heated. Due to the high temperature and oxidizing medium (the stream of the ga-seous ~eat carrier contai~s oxygen), there takes place oxid-ative pyrolysis of heavy tars in the chamber 13. r~his being the case, partial conversion of the li~uid organic compounds occurs, and the gas goes on burninæ. As a result of after-burning of gas and partial burning of the combustibles sepa-rated after the decomposition of heavy tars, the temperature of the heat carrier rises to 1200C~ ~he gaseous heat car-rier together with solid-particles contained therein which have been obtained as a result of thermal processing o~ the pyrogenic water and heavy tars enters -the chamber 7 adap~ed for the second-stage heating of the coal whereupon oxygen of the gaseous heat carrier fully reacts and -che heat carrier the becomes mixed with brown coal being processed which is fed by the feeder 6. Solid particles of the brown coal are whirled by the gaseous stream moving from the centre of the chamber 7 to its periphery through the hot gaseous heat carrier.
The gaseous hea-~ carrier, giving up its heat to the brown coal heats i5 to a temperature of 500-800C. ~his being the case, there takes place an intensive thermal decomposition of the brown coal, giving a vapour-and-gas suspension containing a solid product (coke) in the form of pulverized particles and a vapour-and-gas mixture. ~he ob-cained solid product is ~ ~ 17 ~ ~
discharged from the cnamber 7 adapted for the seconà-stage heating of the brown coal by a turnstile metering device 17.
Simultaneously, the obtained vapour-and-gas mixture is di-scharged into a cyclone (not show~) through a pipe 15 to be purif ied from solid par-ticles. ~'he purified vapour-and-gas suspension is delivered for condensation to yield usable liq-uid products and for separation of low-grade products in the form of heavy tars and pyrogenic water from those usable li~uid products. ~hus obtained lo~J-grade products such as heavy tars and pyrogenic water are directed respectively, into the chamber II and the chamber 13 to be fed into the stream of the gaseous heat carrier.
Example 3rown coal having the calorific value of 3500 kcal/kg, moisture content of ~2 to 38%, ash content of 8% and sulphur content of 0.5% was pulverized until the size of particles was less than one mm, and preheated to a temperature of 110C.
~ he thus obtained brown coal was delivered into chamber I
for heating in a vor-tex stream by a gaseous heat carrier such as stack gas having a temperature of not lower than 500C.
In fractions of a second (about 0.3 sec) the coal ~las heated to a tempera-ture of 200-500C, i.e. to the -tempera-ture at vlhich thermal decomposition of the coal begins. Being heated so fast, the coal practically did not change its com~osition because one ton of the coal being processed yielded but 2~ kg of mass consisting of pyrogenic water, gas and coal carry-off.
~117~49 The s?ant gaseous heat carrier having a temp~rature of about 350 ~as separated from the heated cDal.
leated t~ the temperature o~` the beginnin6r of thermal decomposition, the coal was delivered into chamber 7 adapted for the second-stage heating of the brown coal where was heat-ed by the gaseous heat carrier havi~g a temperature of about 1000C. During 0.3 sec the brown c~al was heated to a tempera-ture of 500-800C. AccDrding to the invention the stream of the gaseous heat carrier cDntaining 100 kg of air per 10 kg of combustible gas was supplied with 50 kg of pyrogenic water per ton. Concurrently with burning o~ gas, there took place evaporation of the water as well as sejaration and oxidative pyrDlysis of organic substances dissolved in the water q'hus, though evaporation o~ the water generally requires about 600 kcal/kg, in this case, due to combustion of phenols dissol-ved in the pyrogenic water, the cDnsumption of energy for t~e evaporation constituted but 150-200 kcaltkg. Furthermore, thermal decomposition of phenols resulted in the formation of an insoluble residue. 75 kg of pulverized heavy tars were in-troduced into chamber 13 through sprayers 14 to be fed into the gaseous heat carrier. Due to the high temperature and oxidi2ing medium (the stream of the gaseous heat carxi~r contained air ox~gen), there took place pyrolysis of the heavy tar, par-tial conversion of liquid organic compounds and combustion of gas of the heat carrier. ~her termal decomposition of the heavy tar resulted in the formation of a solid portion in the form 1~17~49 o~ particles of coke. ~his being the case, the separated com-bus~ibles partia]ly burnt, thereby raising -the temperature o~
the gaseous heat carrier to about 1200C.
Thus the heat carrier comprising products o~ thermal processing of the fuel was delivered in~o the chamber 7 adap-ted for -the second-stage heating, in which chamber the brow~
coal was heated by the obtained gaseous heat carrier to a temperature o~ 500-800C at vJhich the coal was decomposed, thus yieldin$ a vapour-and-gas suspension comprising a solid product in the form of pulverized particles and a vapour and--gas mixture. The vapour--and-gas mixture (a portion) was di-rected for purification and condensation to obtai~ gas, usa-ble liquid products ~nd to separate low-grade products there-from as heavy tars and pyrogenic water~ The low-grade pro-ducts thus obtained were fed into the chamber II and 13 for being processed therein. At the same time the obtained solid product was discharged by a metering device 17 from chamber 7 adapted for the second-stage heating of brown coal.
Realisation of the proposed method, namely pyrolytic processing of heavy tars and pyrogenic water gave 60-80% of the solid product, i.e. 50 kg ~rom 75 kg o~ the h~avy tars.
The solid product having a calorific oapacity of about 8200-8400 kcal/kg was deposited on the product of thermal process-ing of the pulverized brown coal. So, the obtained product comprises the product of thermal processing of the brown coal and product of pyrolytic processing of the heavy tars. Since the calorific capacity of the first from the above-mentioned products is about 6400-~700 kcal/kg and that oi the second above-mentioned product is about 8200-8400 kcal/~g, the total calorific capacity is abou~ 6930 kcal/kg, which is 230 kcaltkg higher than that of the solid product obtained in a conven-tional manner and having the calorific capacity of 6400-6700 kcal/kg. This results in increasing the solid portion by 18%.
Also, it is to be noted that the yield of solid product having an increased calori~ic capacity is achieved withDut any in-crease in the power consumption, i.e. due to the combustion of combustibles which enter into the composition of low-grade products.
Brown coal as the fuel for the process is taken for il-lustration purpose~ only in this particular example. However, it should be evident for those skilled in the art that any other fuel can be used as the process material. With this in view, and according to conventior.al re~uirements, prDcessing of charge fuel as well as low-grade products is carried out at temperature and time operating conditions being maintained in a conventional manner~
.
- 14 _
1~17~
~'rHOD ~OR H~A~ PROC~SSING OF PU~V~RIZ~D
BRO',~ C3A~
The invention relates to methods for the destructive processing o~ solid carbo~-containi~g materials, by breaking down thereof and more specifically, to methods for heat pro-cessing o~ pulverized brown coal~.
~ he invention is o~ particular advantage in energe-tic and chemical industries where it can be used for combined production of hi~h-calorific solid and synthetic liquid fuels as well as other gaseous and liquid producbs whioh are subse-quently processed into technical and chemical raw materials.
Background of bhe Invention There are well known in the art methods for pyrolytic, or heat processing of pulverized solid ~uels by the aid of which both usable products, including solid as well as li~uid products, and loY~-grade products, such as heavy tars and pyr-ogenic water are produced.
on ~ hough the heat o~ combustion of heavy tars, the orderof 8400 k~al/kg, is known to be higher than thab o~ the pro-duct being produced (whose heat of combustion is 6400-6700 kcal/kg), the utilization thereof presents a severe problem.
~his problem derives ~rom the ~act that under normal condi-tions t~r is a sticky viscous substance which is neither too ~luid to be delivered through pipelines nor su~`ficiently solid .. ''~ . , ~, .
to be loaded into and delivered by transporting facilities to the consumer. Consequently, when heavy tar is used as a liquid boiler fuel, it is to be transformed into a liquid by heating, which naturally requires additional capital and operating expenses. Yet here, too, the problem of delivering heavy tars to the consumer stands.
Thus, due to heat processing of fuel, the product whose heat of combustion is 8400 kcal/kg practically cannot be used as fuel.
It is also known that pyrogenic water comprises approxi-mately 4.5% phenols dissolved therein which are usable products.
However, to separate phenols from pyrogenic water, a complicated procedure is to be resorted to, which, again requires considerable capital and operating expenses. In addition, after the separation of phenols from pyrogenic water the latter is to be purified prior to disposal into a water pool.
As a consequence of the fact that world's natural ener-gy resources are running thin, processing of large quantities of low-grade fuels is gaining in importance. Specifically, ever more acute becomes a problem of utilizing heavy tar and pyrogenic water which are low-grade products resulting from heat processing of fuels.
There is known in the art a method for heat processing pulverized brown coal (Inventor's Certificate No. 335267 published in 1972, in Bulletin No. 13 "Discoveries, Inventions, Industrial Designs and Trademarks) comprising a first stage of heating the coal by a gaseous heat carrier in less than one second to a tem-perature of 200-. .
i~l7~
5~0C with subsequent separating of the heat carrier from the coal, a second stage of heating the coal by the gaseous heat carrier in less than one second -to a temperature of 500-800C at which an in-tensive thermal decomposition thereof takes place with the formation of a vapour-and-gas suspension consisting of a solid portion and a vapour-and-gas portion, condensing the vapour-and-gas portion to obtain gas, valuable li~uid products and to separate therefrom low-grade products, such as heavy tars and pyrog~enic water.
'~he re~ization o~ the above method makes it possible to produce along with other usable products also low-grade pro-ducts such as heavy tars and pyrogenic water whose utiliza-tion presents a problem not yet solved.
~ he object of the invention is to provide a method for heat pxocessing of pulverized brown coal, which, with the power input equal to that of the conventional methods ensures the production of a solid product with higher heat combustion.
Another object of the present invention is to provide a method for heat processing of pulverized brown coal, which enables utilization of low-grade products.
One more object of the invention is to provide a method for heat processing pulverized solid ~uel, which makes it possible to realize pyrolytic processing o~ the heavy tar -a product of heat processing o~ brown coal.
Still another object o~ the present invention is to pro-vide a method for processing of pu~verized brown coal, which 7Q~9 ehables utili~ation of org~nic substances dissolved in pyrog-enic v~ater.
Summary of the In~ention ~ hese and o-ther objects are achieved by the pro~ision o~ a method for heat processing of` pulverized brown coal com-prising a first stage of heating the coal by a gaseous heat carrier in less than one second to a temperature of 200-500C
and subsequently separating the spent heat carrier frorn the coal, a second stage o~ heating ~he coal by the gaseous car-rier in less than one second to a tempexature o~ ~00-800C at which temperature an intensive thermal decomposition of the coal takes place with the formation of a vapour-and-gas sus-pension containing a solid portion and a vapour_and-gas por-tion, condensing the vapour-and-gas portion to obtain gas, usable liquid product$ and to separate low-grade products, such as heavy tars and pyrogenic water therefrom, wherein, according to the invention, at the second stage R heating the low-grade products of heat processing of pulverized brown coal are sprayed into the stream of`the gaseous carrier con-taining air oxygen.
It is expedient to supply bhe stream of thc gaseous heat carrier v~ith heavy tar? the oxygen oontent in bhe gaseous car-rier being sufficient for carrying out pyrolybic processing of the heavy tar at predetermined temperatures. Due to pyroly-tic processing of the heavy tar, volatile components are liberat-ed which burn and thereby raise the temperature of ~he gaseous ~ 5 -1~17C~9 heat carrier. In addition, there is formed a solid portion v~hich is a high-calori~ic ~uel.
It is good pxactice to supply the stream of the gaseous heat carrier with pyrogenic water, the gaseous heat carrier being supplied along the stream thereof, first ~ith pyroge-nic water and then with heavy tars, ~his prevents the neces-sity in purifying p~rogenic water prior to disposal thereof into water pools. In addition, organic solvents dissolved in pyrogenic: water can be converted into usable products.
Brie~ Description of the Drawings ~ he above-mentioned and other object o~ this invention will become more apparent-by reference to the following des-cription of an embodiment of the invention taken in conjunc-tion with the accompanying drawing which show~ a diagrammat-ic view of an apparatus for heat processing of pulverized bro~ coal.
Description of the Preferred Embodiment of the Invention ~ ihen realizing the method for heat processing of pulver-ized b~own coal, there is used an apparatus comprizing a chamber 1 adapted ~or the ~irst-stage heating of coal. The apparatus has a hopper 2 communicating with the cha~ber 1 through a turnstile ~eeder 3. A co~nection pipe 4 of a devi-ce ~not shown) ~or feeding ~he gaseous heat carrier t~ngen-tially adaoins the chamber 1. ~o discharge the spent gaseous ~ - 6 -i~7~9 heat carrier, the chamber I is provided with a pipe 5 coa-~ially installed therein and connected with a cyclone (not shown). A chamber 7 adapted ~or the second-stage heating of the ~uel is s~ccesively connected to the chamber I ~hrough a ~eeder 6. Abut-tin~ the cha~ber 7 adapted for the second--stage heating of the coal is a means 8 ~or deli~ering the gaseous heat carrier into ~he chamber 7, the stream of the gaseous heat carrier being supplied with low-grade products.
The means 8 is a pipeline 9 tan~entially adjoining the cham-ber 7 adapted for the second-stage heatin~ of the coal. ~he ~ v.el pipeline 9 is provided with a chamber 10 ~or to be burnt therein a~d -to form stack gas, with chamber II ~or pyrogenic water to be ~ed thereto through sprayers 12, and with a chamber 13 ~or heavy tars to be fed thereto throu~h sprayers 14. '~he chamber 10 incorporates a burner 15 adapted to burn fuel in a mixture with air oxy~en.
To discharge the vapour-and-gas mixture resulting ~rom thermal decomposition of the brown coal, the chamber 7 adap- -ted for the second-stage heating o~ fuel is provided ~ith a pipe 16 coaxially positioned therein and connected with a cyclone (not shown) throu~h a pipeline. Furthermore, the chamber 7 adapted ~or the second-stage heating o~ the brown coal is provided with a turnstile metering device 17 adapted to discharge the obtained solid product ~rom the chamber 7.
According to the invention, the method for heat process-in~ o~ pulverized brown coal is realized as follows.
~17(~49 ~ he pulverized brown coal having the size of prticles below I mm is preheated to a temperature about 110C for dry-ing and is -thereafter fed by the feeder 3 from the hopper 2 into the chamber I adapted for the first-stage heating of the brown c~al. Simultaneously an oxygen-~ree heat carrier in the form o~ stack gas having a temperature o~ no less than 500C
is delivered into t~e chamber I through the connection pipe 4.
~ he heat carrier tangentially enters the chamber I adap-ted for the first-stage heating of the brown coal and draws the particles of the pulverized bxown coal. Under the action o~ centri~ug~al and gravity forces the brown coal particles are thrown towards the wall o~ the chamber and descend in a ~ortex. ~he pulverized brown coal is heated by the heat car-rier to a temperature o~ 200 to 500C. ~he spent gaseous heat carrier cooled down to a temperature about 350C is discharg-ed through the pipe 5 into the cyclone (not shown). A portion of the pulverized brown coal carried away by the heat ca~rier is separated there~rom in a conventional manner.
~ he feeder 6 feeds the brown coal being processed from the chamber I adapted ~or the ~irst stage heating o~ the brown coal into the chamber 7 adapted ~or the second stage heatin~
o~ the brown coal. Concurrently with the coal the gaseous heat carrier is ~ed into the chamber 7 adapted ~or the second--sta~e of heating through the means 8. According to the inven-tion the gaseous heat carrier obtained by burning a fuel, such as gas, and by the ~ormation of stack gas is supplied with low-~117~49 -~rade products. ~his procedure is carried QUt in the follovJ-ing way.
A combustible gas or any other fuel mixed with air oxyg-en is ~ed into a burner 15. Iviore than 50% of the combustible gas is burnt in the chamber 10, thereby forming a gaseous heat carrier containing air oxygen. Since approximately 50%
of combus~ible substance are burn-t in the chamber 10 wherein the heat carrier is ~ormed, the temperature in this chamber reaches about 1200C. It is ~o be noted that the process o~
burning and the temperature in the chamber 10 wherein the heat carrier formation takes place are regulated in a conven-tional manner and by conven~ional means and there~ore should be clear to those skilled in the art. From the chamber 10 wherein the heat carrier formation takes place, the gaseous heat carrier enters the chamber II adapted for processing pyrogenetic water. Simultaneously the stream of ~he gaseous heat carrier is supplied with pyrogenic water through the sprayers 12. In the chamber II adapted for processing pyrog-enic water, there takes place evaporation of the water as well as oxidati~e pyrolysis of organic substances dissolved therein, in particular, phenols. On pyrolysis of or~anic substances, one portion thereof gets transformed, another portion burns, still another is deposited as carbon on pulve-rized particles of the obtained coke. Due to processing of the pyrogenic water, the temperature of the gaseous heat car-rier drops to about 1000C. ~he gaseous heat carrier having _ 9 _ ~17Q~9 the tem~erature of 1000C is fed into the chamber 13 where processing of heavy tars takes place~ The chamber 13 is con-tinuously supplied through the sprayers 14 with heav~ tars which constitute a liquid after being heated. Due to the high temperature and oxidizing medium (the stream of the ga-seous ~eat carrier contai~s oxygen), there takes place oxid-ative pyrolysis of heavy tars in the chamber 13. r~his being the case, partial conversion of the li~uid organic compounds occurs, and the gas goes on burninæ. As a result of after-burning of gas and partial burning of the combustibles sepa-rated after the decomposition of heavy tars, the temperature of the heat carrier rises to 1200C~ ~he gaseous heat car-rier together with solid-particles contained therein which have been obtained as a result of thermal processing o~ the pyrogenic water and heavy tars enters -the chamber 7 adap~ed for the second-stage heating of the coal whereupon oxygen of the gaseous heat carrier fully reacts and -che heat carrier the becomes mixed with brown coal being processed which is fed by the feeder 6. Solid particles of the brown coal are whirled by the gaseous stream moving from the centre of the chamber 7 to its periphery through the hot gaseous heat carrier.
The gaseous hea-~ carrier, giving up its heat to the brown coal heats i5 to a temperature of 500-800C. ~his being the case, there takes place an intensive thermal decomposition of the brown coal, giving a vapour-and-gas suspension containing a solid product (coke) in the form of pulverized particles and a vapour-and-gas mixture. ~he ob-cained solid product is ~ ~ 17 ~ ~
discharged from the cnamber 7 adapted for the seconà-stage heating of the brown coal by a turnstile metering device 17.
Simultaneously, the obtained vapour-and-gas mixture is di-scharged into a cyclone (not show~) through a pipe 15 to be purif ied from solid par-ticles. ~'he purified vapour-and-gas suspension is delivered for condensation to yield usable liq-uid products and for separation of low-grade products in the form of heavy tars and pyrogenic water from those usable li~uid products. ~hus obtained lo~J-grade products such as heavy tars and pyrogenic water are directed respectively, into the chamber II and the chamber 13 to be fed into the stream of the gaseous heat carrier.
Example 3rown coal having the calorific value of 3500 kcal/kg, moisture content of ~2 to 38%, ash content of 8% and sulphur content of 0.5% was pulverized until the size of particles was less than one mm, and preheated to a temperature of 110C.
~ he thus obtained brown coal was delivered into chamber I
for heating in a vor-tex stream by a gaseous heat carrier such as stack gas having a temperature of not lower than 500C.
In fractions of a second (about 0.3 sec) the coal ~las heated to a tempera-ture of 200-500C, i.e. to the -tempera-ture at vlhich thermal decomposition of the coal begins. Being heated so fast, the coal practically did not change its com~osition because one ton of the coal being processed yielded but 2~ kg of mass consisting of pyrogenic water, gas and coal carry-off.
~117~49 The s?ant gaseous heat carrier having a temp~rature of about 350 ~as separated from the heated cDal.
leated t~ the temperature o~` the beginnin6r of thermal decomposition, the coal was delivered into chamber 7 adapted for the second-stage heating of the brown coal where was heat-ed by the gaseous heat carrier havi~g a temperature of about 1000C. During 0.3 sec the brown c~al was heated to a tempera-ture of 500-800C. AccDrding to the invention the stream of the gaseous heat carrier cDntaining 100 kg of air per 10 kg of combustible gas was supplied with 50 kg of pyrogenic water per ton. Concurrently with burning o~ gas, there took place evaporation of the water as well as sejaration and oxidative pyrDlysis of organic substances dissolved in the water q'hus, though evaporation o~ the water generally requires about 600 kcal/kg, in this case, due to combustion of phenols dissol-ved in the pyrogenic water, the cDnsumption of energy for t~e evaporation constituted but 150-200 kcaltkg. Furthermore, thermal decomposition of phenols resulted in the formation of an insoluble residue. 75 kg of pulverized heavy tars were in-troduced into chamber 13 through sprayers 14 to be fed into the gaseous heat carrier. Due to the high temperature and oxidi2ing medium (the stream of the gaseous heat carxi~r contained air ox~gen), there took place pyrolysis of the heavy tar, par-tial conversion of liquid organic compounds and combustion of gas of the heat carrier. ~her termal decomposition of the heavy tar resulted in the formation of a solid portion in the form 1~17~49 o~ particles of coke. ~his being the case, the separated com-bus~ibles partia]ly burnt, thereby raising -the temperature o~
the gaseous heat carrier to about 1200C.
Thus the heat carrier comprising products o~ thermal processing of the fuel was delivered in~o the chamber 7 adap-ted for -the second-stage heating, in which chamber the brow~
coal was heated by the obtained gaseous heat carrier to a temperature o~ 500-800C at vJhich the coal was decomposed, thus yieldin$ a vapour-and-gas suspension comprising a solid product in the form of pulverized particles and a vapour and--gas mixture. The vapour--and-gas mixture (a portion) was di-rected for purification and condensation to obtai~ gas, usa-ble liquid products ~nd to separate low-grade products there-from as heavy tars and pyrogenic water~ The low-grade pro-ducts thus obtained were fed into the chamber II and 13 for being processed therein. At the same time the obtained solid product was discharged by a metering device 17 from chamber 7 adapted for the second-stage heating of brown coal.
Realisation of the proposed method, namely pyrolytic processing of heavy tars and pyrogenic water gave 60-80% of the solid product, i.e. 50 kg ~rom 75 kg o~ the h~avy tars.
The solid product having a calorific oapacity of about 8200-8400 kcal/kg was deposited on the product of thermal process-ing of the pulverized brown coal. So, the obtained product comprises the product of thermal processing of the brown coal and product of pyrolytic processing of the heavy tars. Since the calorific capacity of the first from the above-mentioned products is about 6400-~700 kcal/kg and that oi the second above-mentioned product is about 8200-8400 kcal/~g, the total calorific capacity is abou~ 6930 kcal/kg, which is 230 kcaltkg higher than that of the solid product obtained in a conven-tional manner and having the calorific capacity of 6400-6700 kcal/kg. This results in increasing the solid portion by 18%.
Also, it is to be noted that the yield of solid product having an increased calori~ic capacity is achieved withDut any in-crease in the power consumption, i.e. due to the combustion of combustibles which enter into the composition of low-grade products.
Brown coal as the fuel for the process is taken for il-lustration purpose~ only in this particular example. However, it should be evident for those skilled in the art that any other fuel can be used as the process material. With this in view, and according to conventior.al re~uirements, prDcessing of charge fuel as well as low-grade products is carried out at temperature and time operating conditions being maintained in a conventional manner~
.
- 14 _
Claims (3)
1. A method for heat processing of pulverized brown coal, comprising the following operations: a first stage of heating brown coal by a gaseous heat carrier in less than one second to a temper-ature of 200-500°C, separating the gaseous heat carrier from the brown coal, a second stage of heating the brown coal by the gaseous heat carrier in less than one second to a temperature of 500-800°C
at which temperature thermal decomposition of the brown coal takes place with the formation of a vapour-and-gas suspension, breaking the obtained vapour-and-gas suspension into a solid matter and a vapour-and-gas portion; condensing the vapour-and-gas portion to obtain gas, usable liquid products and to separate low-grade products therefrom, such as heavy tars and pyrogenic water; supply-ing air oxygen and spraying low-grade products of heat processing of the pulverized brown coal into the stream of the gaseous heat carrier at said second stage of heating the brown coal.
at which temperature thermal decomposition of the brown coal takes place with the formation of a vapour-and-gas suspension, breaking the obtained vapour-and-gas suspension into a solid matter and a vapour-and-gas portion; condensing the vapour-and-gas portion to obtain gas, usable liquid products and to separate low-grade products therefrom, such as heavy tars and pyrogenic water; supply-ing air oxygen and spraying low-grade products of heat processing of the pulverized brown coal into the stream of the gaseous heat carrier at said second stage of heating the brown coal.
2. A method as claimed in claim 1, wherein the stream of the gaseous heat carrier fed at said second stage of heating the brown coal is supplied with heavy tars for carrying out pyrolytic processing thereof.
3. A method as claimed in claim 1 and 2, wherein the stream of the gaseous heat carrier fed at said second stage of heating the brown coal is supplied with pyrogenic water, the gas heat carrier being at the same time supplied along its stream, first with pyro-genic water and then with heavy tars.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000308624A CA1117049A (en) | 1978-08-02 | 1978-08-02 | Method for heat processing of pulverized brown coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000308624A CA1117049A (en) | 1978-08-02 | 1978-08-02 | Method for heat processing of pulverized brown coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1117049A true CA1117049A (en) | 1982-01-26 |
Family
ID=4112048
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000308624A Expired CA1117049A (en) | 1978-08-02 | 1978-08-02 | Method for heat processing of pulverized brown coal |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1117049A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012059938A1 (en) * | 2010-11-02 | 2012-05-10 | Keki Hormusji Gharda | Process for obtaining petrochemical products from carbonaceous feedstock |
-
1978
- 1978-08-02 CA CA000308624A patent/CA1117049A/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012059938A1 (en) * | 2010-11-02 | 2012-05-10 | Keki Hormusji Gharda | Process for obtaining petrochemical products from carbonaceous feedstock |
| CN103237868A (en) * | 2010-11-02 | 2013-08-07 | 凯基·霍尔穆斯吉·格哈达 | Process for obtaining petrochemical products from carbonaceous feedstock |
| US8696937B2 (en) | 2010-11-02 | 2014-04-15 | Keki Hormusji Gharda | Process for obtaining petrochemical products from carbonaceous feedstock |
| EA023138B1 (en) * | 2010-11-02 | 2016-04-29 | Кеки Хормусджи Гхарда | Process for obtaining petrochemical products from carbonaceous feedstock |
| AU2011324788B2 (en) * | 2010-11-02 | 2016-05-26 | Keki Hormusji Gharda | Process for obtaining petrochemical products from carbonaceous feedstock |
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