CN103013546A - Method for realizing oil shale refining and boiler combustion with steam cogeneration by integrating novel oil shale refining with differential fluidized bed combustion - Google Patents

Abstract

The invention discloses a method for realizing oil shale refining and boiler combustion with steam cogeneration by integrating novel oil shale refining with differential fluidized bed combustion. The method comprises the following steps of: crushing and screening oil shale ore and conveying qualified oil shale ore into a multi-pipe drum carbonization device on two sides of a boiler to prepare shale oil and fuel gas; directly conveying generated high-temperature oil shale semicoke into the differential fluidized bed boiler through a material conveying device to burn; converting generated hot smoke into steam and using the steam as a hot medium of the carbonization to enter the multi-pipe drum carbonization device; and returning the carbonized smoke to the boiler.

Description

Novel oil shale oil-refining and differential fluidized-bed combustion integrated boiler are realized the method for oil shale oil-refining and boiler combustion coproduction steam

Technical field

The present invention relates to a kind of method that realizes oil shale oil-refining and boiler combustion coproduction steam, relate in particular to the method that a kind of novel oil shale oil-refining and differential fluidized-bed combustion integrated boiler are realized oil shale oil-refining and boiler combustion coproduction steam.

Background technology

At present, there is following problem in resinous shale in the utilization of oil refining with boiler combustion:

1, present comparatively ripe oil shale oil-refining method is mainly processed the 15-80mm resinous shale, can't directly process for the 0-12mm oil shale particle, is in to be abandoned or directly burning, has lost shale oil, can not utilize to greatest extent oil shale resources;

2, the high temperature semicoke of gas retort discharge can't directly enter circular fluid bed, needs intercooling with broken, the comprehensive utilization weak effect of resinous shale;

3, the dry distillation medium of at present circulating fluidized bed gas retort employing is the thermal cycling ash, yet adopt circulating ash as dry distillation medium so that contain a large amount of dirt ashes in shale oil and the combustion gas, this dirt ash content that has increased shale oil and combustion gas has also limited shale oil and combustion gas and has used from difficulty and cost;

4, oil refining and the boiler coal-char combustion of most of oil shale are respectively independently to finish in gas retort and the circular fluid bed, do not become one at present, easily cause secondary pollution.

Summary of the invention

The purpose of this invention is to provide a kind of novel oil shale oil-refining and differential fluidized-bed combustion integrated boiler and realize the method for oil shale oil-refining and boiler combustion coproduction steam, it can be finished oil refining and the differential fluidized-bed boiler combustion integrative of resinous shale, utilizes to greatest extent oil shale resources.

The present invention is achieved like this, fast method realize in the steps below:

Step 1: the resinous shale of 0-12mm is by pipe or the Polygons tube interior of feeder input multitube cylinder destructive distillation device after pulverizing, be heated to 150-200 ℃ through preheating section, behind the dry moisture of resinous shale, entering retort section is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, produce the shale oil carbonization gas, enter the shale oil condenser by the outlet of shale oil carbonization gas, isolate shale oil and inflammable gas;

Step 2: the low-temperature flue gas of discharging behind the boiler economizer is through the low-temperature flue gas fairlead, draw the low-temperature flue gas import that 200-250 ℃ of low-temperature flue gas enters multitube cylinder destructive distillation device preheating section to both sides, resinous shale is through entering fly-ash separator by the low-temperature flue gas outlet after the preheating; The 700-800 ℃ of high-temperature flue gas of drawing behind the furnace outlet high temperature superheater, enter multitube cylinder destructive distillation device retort section by high-temperature flue gas fairlead and high-temperature flue gas import, high-temperature flue gas is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, and the flue gas process high-temperature flue gas outlet after cold lacking and high-temperature flue gas draw return pipe and draw the back boiler back-end surfaces; The high and low temperature flue gas is to walk outside the pipe of the inner pipe of multitube cylinder destructive distillation device or Polygons pipe in multitube cylinder destructive distillation device preheating section and retort section, does not directly contact with resinous shale;

Step 3: high temperature oil shale semicockes and combustion-supporting fuel enter burner hearth by feeding device with negative pressure mode, drop in the middle aerofoil;

Step 4: adopt the high-low pressure secondary blast: high-pressure blast forms the 3-5m/s fluidising air velocity by middle air compartment and middle aerofoil emulsion zone thereon, and heating surface is not arranged in this emulsion zone position; Low-pressure air forms the 1.5-2.5m/s fluidising air velocity by both sides air compartment and both sides aerofoil emulsion zone thereon, and this emulsion zone location arrangements pipe laying heating surface is conducive to control the siege temperature, and because the low wearing and tearing of also having avoided pipe laying of wind speed; The 300-500mm discrepancy in elevation of middle aerofoil and both sides aerofoil and fluidising air velocity are poor to form internal recycle stream at emulsion zone jointly;

Step 5: fuel generates 800-900 ℃ of flue gas in the burner hearth internal combustion, at first pass through the high temperature superheater of furnace outlet, flue-gas temperature is reduced to 700-800 ℃ and is drawn through both sides respectively and enter multitube cylinder destructive distillation device retort section, then drawing return pipe by high-temperature flue gas draws back, be down to 200-250 ℃ through low temperature superheater and economizer flue-gas temperature, enter respectively both sides multitube cylinder destructive distillation device preheating section by both sides low-temperature flue gas fairlead and low-temperature flue gas import again, flue gas enters fly-ash separator by the low-temperature flue gas outlet behind the preheat oil shale.

Technique effect of the present invention is: multitube cylinder destructive distillation device can directly be processed 0-12mm oil page or leaf particle, produces the not carbonization gas of dust-laden; High temperature semicoke waste directly enters the burning of differential fluidized boiler by feeding device, avoids energy dissipation and secondary pollution, and the heat of generation is converted into steam and is used for generating electricity and heat supply.Multitube cylinder destructive distillation device is divided into anterior preheating section and rear portion retort section, enter retort section from the high-temperature flue gas of differential fluidized-bed high temperature superheater outlet, after then flue gas is got back to the heated surface at the end of boiler heat transfer, enter again multitube cylinder destructive distillation device preheating section, enter at last fly-ash separator.Resinous shale does not directly contact with the thermal medium flue gas in the multitube cylinder destructive distillation device, and resinous shale is walked in the pipe, and the thermal medium flue gas is walked outside the pipe, can avoid the destructive distillation band of gas dirt produced, has to utilize to isolate clean shale oil and combustion gas.High temperature semicoke after the destructive distillation directly enters again back boiler of fluidized boiler burning and high low-temperature flue gas after the destructive distillation of multitube cylinder destructive distillation device, is energy-conservation again environmental protection like this.

Description of drawings

Fig. 1, Fig. 2 are fundamental diagram of the present invention.

Among the figure: air compartment in the middle of 1, aerofoil in the middle of the 1-1,2 both sides air compartments, 2-1 both sides aerofoil, 3 pipe layings, 4 material inlets, 5 differential fluidized-bed boilers, 6 high-temperature flue gas fairleads, the import of 6-1 high-temperature flue gas, 7 high-temperature flue gas draw return pipe, the outlet of 7-1 high-temperature flue gas, 8 high low temperature superheaters, the 8-1 high temperature superheater, the 8-2 low temperature superheater, 9 economizers, 10 low-temperature flue gas fairleads, the import of 10-1 low-temperature flue gas, 11 feeders, 12 multitube cylinder destructive distillation devices, 12-1 multitube cylinder destructive distillation device preheating section, 12-2 multitube cylinder destructive distillation device retort section, the outlet of 13 low-temperature flue gas, 14 warm sludge feeding devices, the outlet of 15 shale oil carbonization gas.

Embodiment

As shown in Figure 1 and Figure 2, the present invention includes multitube cylinder destructive distillation device, feeder, feeding device, differential fluidized-bed boiler etc.During use, resinous shale is sent into multitube cylinder destructive distillation device preheating section and is carried out preheating through after being crushed to 0-12mm, after enter retort section and carry out destructive distillation, pyrolysis temperature 450-500 ℃, the carbonization gas that destructive distillation produces enters condensing works, isolates shale oil and combustion gas; The high temperature that produces in the oil shale distillation process (450-500 ℃) semicoke directly enters the differential fluidized-bed boiler burning by feeding device, and temperature of combustion is 800-900 ℃, and the heat of generation is converted into steam, can be used to generating and heat supply; As the destructive distillation thermal medium, ℃ flue gas of the 550-650 after the destructive distillation returns in the differential fluidized-bed boiler by flue the retort section of 700-800 ℃ of high-temperature flue gas introducing multitube cylinder destructive distillation device behind differential fluidized-bed boiler furnace outlet flue gas process high temperature superheater.Boiler enters 200-250 ℃ front flue gas of fly-ash separator again by the preheating section in the flue introducing destructive distillation device, and resinous shale is carried out preheating; Last smoke evacuation enters fly-ash separator and enters chimney again.

Said process by the following method step is finished:

[0014] step 1: the resinous shale of 0-12mm is by pipe or the Polygons tube interior of feeder (11) input multitube cylinder destructive distillation device (12) after pulverizing, be heated to 150-200 ℃ through preheating section, behind the dry moisture of resinous shale, entering retort section is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, produce the shale oil carbonization gas, enter the shale oil condenser by shale oil carbonization gas outlet (15), isolate shale oil and inflammable gas.

Step 2: the low-temperature flue gas of discharging behind the boiler economizer is through low-temperature flue gas fairlead (10), draw the low-temperature flue gas import (10-1) that 200-250 ℃ of low-temperature flue gas enters multitube cylinder destructive distillation device preheating section (12-1) to both sides, resinous shale is through entering fly-ash separator by low-temperature flue gas outlet (13) after the preheating; The 700-800 ℃ of high-temperature flue gas of drawing behind the furnace outlet high temperature superheater, enter multitube cylinder destructive distillation device retort section (12-2) by high-temperature flue gas fairlead (6) and high-temperature flue gas import (6-1), high-temperature flue gas is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, and the flue gas process high-temperature flue gas outlet (7-1) after cold lacking and high-temperature flue gas draw return pipe (7) and draw the back boiler back-end surfaces; The high and low temperature flue gas is to walk outside the pipe of the inner pipe of multitube cylinder destructive distillation device or Polygons pipe in multitube cylinder destructive distillation device preheating section and retort section, does not directly contact with resinous shale.

Step 3: high temperature oil shale semicockes and combustion-supporting fuel enter burner hearth by feeding device (14) with negative pressure mode, drop in the middle aerofoil (1-1).

Step 4: adopt the high-low pressure secondary blast: high-pressure blast forms the 3-5m/s fluidising air velocity by middle air compartment (1) and middle aerofoil (1-1) emulsion zone thereon, and heating surface is not arranged in this emulsion zone position; Low-pressure air forms the 1.5-2.5m/s fluidising air velocity by both sides air compartment (2) and both sides aerofoil (2-1) emulsion zone thereon, this emulsion zone location arrangements pipe laying (3) heating surface, be conducive to control the siege temperature, and because the low wearing and tearing of also having avoided pipe laying (3) of wind speed; Middle aerofoil (1-1) is poor jointly at emulsion zone formation internal recycle stream with the 300-500mm discrepancy in elevation and the fluidising air velocity of both sides aerofoil (2-1).

Step 5: fuel generates 800-900 ℃ of flue gas in the burner hearth internal combustion, at first pass through the high temperature superheater (8-1) of furnace outlet, flue-gas temperature is reduced to 700-800 ℃ and is drawn through both sides respectively and enter multitube cylinder destructive distillation device retort section (12-2), then drawing return pipe (7) by high-temperature flue gas draws back, be down to 200-250 ℃ through low temperature superheater (8-2) and economizer (9) flue-gas temperature, enter respectively both sides multitube cylinder destructive distillation device preheating sections (12-1) by both sides low-temperature flue gas fairleads (10) and low-temperature flue gas import (10-1) again, flue gas enters fly-ash separator by low-temperature flue gas outlet (13) behind the preheat oil shale.

Step 6: when the resinous shale calorific value not little, in the time of can't making the boiler balance through semicoke total heat after the destructive distillation, cause bed temperature on the low side, can't meet the demands, can carry out balance by aerofoil (1-1) interpolation resinous shale or other fuel mode in the middle of boiler, improve bed temperature.

Claims (1)

1. a novel oil shale oil-refining and differential fluidized-bed combustion integrated boiler are realized the method for oil shale oil-refining and boiler combustion coproduction steam, it is characterized in that: fast method realize in the steps below:

Step 1: the resinous shale of 0-12mm is by pipe or the Polygons tube interior of feeder (11) input multitube cylinder destructive distillation device (12) after pulverizing, be heated to 150-200 ℃ through preheating section, behind the dry moisture of resinous shale, entering retort section is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, produce the shale oil carbonization gas, enter the shale oil condenser by shale oil carbonization gas outlet (15), isolate shale oil and inflammable gas;

Step 2: the low-temperature flue gas of discharging behind the boiler economizer is through low-temperature flue gas fairlead (10), draw the low-temperature flue gas import (10-1) that 200-250 ℃ of low-temperature flue gas enters multitube cylinder destructive distillation device preheating section (12-1) to both sides, resinous shale is through entering fly-ash separator by low-temperature flue gas outlet (13) after the preheating; The 700-800 ℃ of high-temperature flue gas of drawing behind the furnace outlet high temperature superheater, enter multitube cylinder destructive distillation device retort section (12-2) by high-temperature flue gas fairlead (6) and high-temperature flue gas import (6-1), high-temperature flue gas is heated to 450-500 ℃ of pyrolysis temperature with resinous shale and carries out destructive distillation, and the flue gas process high-temperature flue gas outlet (7-1) after cold lacking and high-temperature flue gas draw return pipe (7) and draw the back boiler back-end surfaces; The high and low temperature flue gas is to walk outside the pipe of the inner pipe of multitube cylinder destructive distillation device or Polygons pipe in multitube cylinder destructive distillation device preheating section and retort section, does not directly contact with resinous shale;

Step 3: high temperature oil shale semicockes and combustion-supporting fuel enter burner hearth by feeding device (14) with negative pressure mode, drop in the middle aerofoil (1-1);

Step 4: adopt the high-low pressure secondary blast: high-pressure blast forms the 3-5m/s fluidising air velocity by middle air compartment (1) and middle aerofoil (1-1) emulsion zone thereon, and heating surface is not arranged in this emulsion zone position; Low-pressure air forms the 1.5-2.5m/s fluidising air velocity by both sides air compartment (2) and both sides aerofoil (2-1) emulsion zone thereon, this emulsion zone location arrangements pipe laying (3) heating surface, be conducive to control the siege temperature, and because the low wearing and tearing of also having avoided pipe laying (3) of wind speed; Middle aerofoil (1-1) is poor jointly at emulsion zone formation internal recycle stream with the 300-500mm discrepancy in elevation and the fluidising air velocity of both sides aerofoil (2-1);

Step 5: fuel generates 800-900 ℃ of flue gas in the burner hearth internal combustion, at first pass through the high temperature superheater (8-1) of furnace outlet, flue-gas temperature is reduced to 700-800 ℃ and is drawn through both sides respectively and enter multitube cylinder destructive distillation device retort section (12-2), then drawing return pipe (7) by high-temperature flue gas draws back, be down to 200-250 ℃ through low temperature superheater (8-2) and economizer (9) flue-gas temperature, enter respectively both sides multitube cylinder destructive distillation device preheating sections (12-1) by both sides low-temperature flue gas fairleads (10) and low-temperature flue gas import (10-1) again, flue gas enters fly-ash separator by low-temperature flue gas outlet (13) behind the preheat oil shale.

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