CA2907624A1

CA2907624A1 - An apparatus and a process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass

Info

Publication number: CA2907624A1
Application number: CA2907624A
Authority: CA
Inventors: Jianxiang HE
Original assignee: Individual
Current assignee: Individual
Priority date: 2013-03-21
Filing date: 2014-02-10
Publication date: 2014-09-25
Anticipated expiration: 2034-02-10
Also published as: WO2014146520A1; CN103160301B; CA2907624C; CN103160301A

Abstract

The present invention discloses an apparatus and a process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass. The apparatus includes a conveying device, a storage bin, a metering device, a drying furnace and a surge bin, which are connected sequentially, and the process includes drying and preheating, dry distilling and cooling. An externally-heated rotary dry distillation furnace is provided as a core apparatus of the invention for the pyrolysis of oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale and biomass, producing products of high purity with little loss and effectively solving the adhesion and wall sticking problem of solid materials during the pyrolysis process by returning materials. The process of simplified and stable operation has a distinct advantage in processing granular materials, including oil sand, oil sludge (e.g.
mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale and biomass.

Description

An apparatus and a process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass Technical field of the invention This invention, belonging to the technical field of energy development, relates to a system and a process for the low-temperature pyrolysis (or dry distilling) of solid material, in particular to a system and a process of pyrolyzing (or dry distilling) oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale and biomass (xylon, straw, solid waste and etc.) with an externally-heated rotary furnace as a core apparatus.
Background of the invention Percentage of oil reserves is less than 5% and percentage of natural gas is only 0.3% of total energy reserves in China. Shortage of oil and natural gas becomes a remarkable problem impacting economic development. Therefore, increasing attention is paid to the development of unconventional oil and gas energy in recent years which has become new economic development pole.
Pyrolysis techniques for oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale, biomass (e.g. xylon, straw, solid waste) and other solid material in the world mainly are the technologies of internally-heated vertical furnace, externally-heated vertical furnace, solid heat carrier, fluidized bed. Despite the advantages of simplified technology and less investment, internally-heated vertical heaters have a low usage rate of raw materials, a yield of impure coal gas, severer pollution, a lower yield rate of tar and the like.
Other techniques also have the disadvantages of redundant technology, complicated equipment and low running rate, whereby the techniques fail to realize the overall industrialization.
Summary of the invention It is an object of the present invention to provide a process with an externally-heated rotary dry distillation (or pyrolysis) furnace as a core apparatus for low-temperature dry distillation (or pyrolysis) of oil sand, oil sludge, oil shale and biomass which overcomes the above-described disadvantages of the prior art.
The process of simplified technology and stable operation has a distinct advantage in processing oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale and biomass (e.g. xylon, straw, solid waste) and other granulated materials.
The objects of the invention are accomplished by the following technical scheme:
An apparatus for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass comprises a conveying device, a stock bin connected to the conveying device, and a metering device connected to the stock bin, the metering device is connected to a drying furnace and a surge bin respectively, the metering device is connected to a drying furnace via a 1# feeding airlock device, the drying furnace is connected to the surge bin via a 1# discharging airlock device; and the surge bin is connected to a rotary dry distillation furnace and a cooling device in sequence, the surge bin is connected to the rotary dry distillation furnace via a 2# feeding airlock device, the rotary dry distillation furnace is connected to the cooling device via a 2#
discharging airlock device.
Further, in the apparatus:
The rotary dry distillation furnace is connected to a pyrolysis gas processing system and a dry distillation heating system.
The rotary dry distillation furnace comprises a rotary cylinder supported by a supporting device, and the rotary cylinder comprises a front part of the furnace body, a heating section of the rotary furnace body and a discharging end connected in sequence; the front part of the furnace body is provided with a feeding end, a gas outlet and a gearing;
the heating section of the rotary furnace body comprises three sections, internal heating tubes are arranged along the inside of the three sections, heat source outlets are arranged at a front section and a middle section of the heating section respectively, heat source inlets are arranged at the middle section and an end section of the heating section respectively; and the rotary dry distillation furnace is provided with an external material-returning device and an internal material-returning device.
The dry distillation heating system comprises a combustion device and an air

2 ' CA 02907624 2015-09-21 distribution device connected to the heat source outlets and arranged on the combustion device; a front end of the combustion device communicates with the heat source inlets and a tail end of the combustion device communicates with an end of the pyrolysis gas fuel;
a tail-end air inlet pipeline of the combustion device communicates with a waste-heat recovery device, the waste-heat recovery device is communicated with a fume extractor and a combustion-supporting air pipeline respectively; and a hot flue gas circulating device is arranged on the air inlet pipeline which connects the air distribution device and the heat source outlets.
The cooling device comprises a cylinder supported by a supporting device, the heat exchanging tubes arranged inside the cylinder, a cooling shell side is formed between an outer wall of the cylinder and the heat exchanging tubes; a feeding end is arranged at the front end of the cylinder and a discharging end is arranged at a tail end of the cylinder, the discharging end is connected to a cooling medium inlet via a rotary joint where a cooling medium outlet is arranged; a gearing is arranged on the cylinder.
Accordingly, the invention also provides a process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass comprising the following steps:
1) raw oil sand, oil sludge, oil shale or biomass is crushed and sieved to the required particle size and delivered to a raw materials stock bin by a conveying device, and then to the drying furnace through a 1# feeding airlock device after the measurement by a metering device; drying furnace works by means of hot flue gas drying or steam pipe drying, of which demanded heat is supplied by the drying furnace heating system which mainly comprises a combustion device, an air distribution device, a dust-extraction device, a fume extractor and a hot flue gas circulating device; final temperature of dehydrated and preheated materials is ranging from 80 C to 150 C;
2) the dehydrated and preheated raw materials is delivered to a surge bin through a 1# discharging airlock device, and then to a rotary dry distillation furnace through a 2# feeding airlock device;

3) the materials in the rotary dry distillation furnace is heated and dry distilled by =
' CA 02907624 2015-09-21 -hot flue gas in an external heating jacket or/and internal heating tubes; a mixing device or a material-returning device is provided for dry distillation before the rotary dry distillation furnace if the raw material is of high viscosity and poor fluidity; certain temperature and micro-positive pressure or micro-negative pressure is maintained inside the rotary dry distillation furnace 11 and the produced hot pyrolysis gas is sent to a tail gas treatment process to separate and recycle the components thereof; and

4) the solid pyrolysis products are discharged out of a furnace body through a discharging end of the rotary dry distillation furnace, and are delivered through a 2#
discharging airlock device and to a cooling device 9 via a feeding end 9-5, and then to a shell side of a cooler 9-3, after that the solid pyrolysis products are delivered to next process or packaged to product after cooling.
Further, in the process:
The raw materials unnecessarily dehydrated and preheated are delivered directly from the surge bin to the rotary dry distillation furnace through the feeding airlock device after measurement.
In step 3, in the rotary dry distillation furnace, the reaction time of the materials is ranging from 30 to 120 minutes, final reaction temperature is ranging from 300 C to 700 C, micro-positive or micro-negative pressure is maintained and pressure value is ranging from -500 mm H20 to 500 mm H20.
In step 3, a mixing device is arranged before the rotary dry distillation furnace to mix sand, ceramic ball, ceramic particle or solid pyrolysis products with raw material which is of high viscosity and poor fluidity at the weight rate of 1-2:1, or solid pyrolysis products are delivered to the mixing device by a conveying device and mixed with the raw material which is of high viscosity and poor fluidity at the weight rate of 1-2:1.
In step 3, the material-returning device is provided for dry distillation if the raw material is of high viscosity and poor fluidity, the internal material-returning device or the external material-returning device is arranged to return solid pyrolysis products to the feeding end to mix with the raw material which is of high viscosity and poor fluidity at the weight ratio of 1-2:1.
The technical innovations of the invention are as follows:
1) The raw material: External heating rotary furnace has the capability of processing solid materials with particle size of less than 30 mm which is unable to be processed by existing traditional techniques;
2) Highly utilization of heat: Heat utilization is high as the result of cyclic utilizing high-temperature flue gas, recovering waste heat of discharged flue gas, recovering waste heat of tailings, reducing energy consumption and saving water by comparison with coke wet quenching, and generating steam by steam boiler from delivered process water;
3) Processing capacity of single set of apparatus is able to achieve 1,000,000 tons raw material per year;
4) The apparatus is flexible to operate, as technological parameters are easy to adjust and the yields of each product can be adjusted and controlled according to the changes of market;

5) The apparatus is of high degree of automation, reliable running and stable operation so as to effectively reduce the fixed number of staff members of the apparatus;

6) High-quality products:
a. Semi-coke is waterless by using continuous dry quenching, which improves the quality of solid products and has a distinct advantage in environmental protection, including saving water, and reducing noxious gas and industrial waste water;
b. Produced oil is of high quality and productive rate, of which density is low and light fraction content is high, percentage composition of H element is over 9%
and is capable of serving as high-quality raw material of hydrogenation, liquid products yield rate reaches over 90% by Gray-king assay because of high controllability of final heating temperature and temperature rise rate; and c. Coal gas is of high purity and calorific value, of which effective constituents of CH4, H2. CO content is high and content of N2 is lower than 2%, heat value is over 4800 kcal/Nm3, and is capable of serving as high-quality feed gas for producing natural gas, synthesis methanol and synthesis ammonia, and extracting hydrogen and the like;

7) The process has wide range of application, thus different scheme and parameters are applied to different materials;

8) The process effectively solves processing problem of cohesive materials;

9) Material is mixed continuously, stably, evenly and automatically.

Brief description of the drawings Figure 1 is production process flow of this invention.
Figure 2 is a schematic diagram of an externally-heated rotary dry distillation furnace.
Figure 3 is a schematic diagram of an external material-returning pattern.
Figure 4 is a schematic diagram of an internal material-returning pattern.
Figure 5 is a schematic diagram of a cooling device for solid pyrolysis products.
Figure 6 is a schematic diagram of a dry distillation heating system.
In the drawings:
11-4 ¨ External Heating 1 ¨ Conveying Device 9-1 ¨ Cooling Medium Inlet Jacket 2¨ Stock Bin 9-2 ¨ Rotary Joint 11-5 ¨ Rotary Shell 3 ¨ Metering Device 9-3¨A Shell Side Of A Cooler 11-6 ¨ Discharging End 4 ¨ 1# Feeding Airlock Device 9-4 ¨ Heat Transfer Tubes 11-7 ¨ Heat Source Inlets 5¨ Drying Heating system 9-5 ¨ Feeding End 11-8 ¨ Internal Heating Tubes 6 ¨ Surge Bin 9-6 ¨ Gearing 11-9 ¨ Supporting Device 7 ¨ 2# Feeding Airlock Device 9-7 ¨ Supporting Device 11-10 ¨ Gearing 8 ¨ Dry distillation heating 11-11 ¨ External 9-8 ¨Discharging End system Material-Returning Device 11-12 ¨ Internal 8-1 ¨ Combustion Device 9-9 ¨ Cooling Medium Outlet Material-Returning Device 8-2 ¨Air Distribution Device 10 ¨2# Discharging Airlock 12 ¨Pyrolysis Gas Device Processing System 8-3 ¨ Fume Extractor 11 ¨ Rotary Dry Distillation 13 ¨ 1#
Discharging Airlock Furnace Device 8-4 ¨ Waste-Heat Utilization device 11-1 ¨ Feeding End 14 ¨ Drying Furnace 8-5 ¨ Hot Flue Gas Circulating 11-2 ¨ Gas Outlet Device 9 ¨ Cooling Device 11-3 ¨ Heat Source Outlets Detailed description of the embodiments Detailed description of the invention is illustrated by embodiments with accompanying figures.
Figure 1 is a structure diagram of the apparatus in the invention.
An apparatus for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass is provided. The apparatus comprises a conveying device 1, a stock bin 2 and a metering device 3 connected in sequence. The metering device 3 is connected to a drying furnace 14 and a surge bin 6 respectively; the metering device 3 is connected to the drying furnace 14 via a 1# feeding airlock device 4, the drying furnace 14 is connected to the surge bin 6 via a 1# discharging airlock device 13; and the surge bin 6 is connected to a rotary dry distillation furnace 11 and a cooling device 9 in sequence, the surge bin 6 is connected to the rotary dry distillation furnace 11 via a 2# feeding airlock device 7, the rotary dry distillation furnace 11 is connected to the cooling device 9 via a 2# discharging airlock device 10. A drying heating system 5 is communicated with the drying furnace 14 which works by means of hot flue gas drying or steam pipe drying and of which the demanded heat supplied by the drying heating system, the drying furnace 14 mainly comprises a combustion device, an air distribution device, a dust-extraction device, a fume extractor and a hot flue gas circulating device; and the rotary dry distillation furnace 11 is connected to a pyrolysis gas processing system 12 and a dry distillation heating system 8.
Belt conveyor, chain scraper (or chain bucket) conveyor, bucket elevator or the like is available as conveying device, and the belt conveyor is preferably.
Belt scale, screw scale, weight loss scale or the like is available as the metering device, and the belt scale is preferably. Drying furnace heating system works by means of hot flue gas drying or steam pipe drying, of which the demanded heat is supplied by the drying furnace heating system which could be the hot blast system for producing hot flue gas by burning solid, liquid or gas fuels, or could be the boiler system for producing steam by burning solid, liquid or gas fuels to match different drying furnace types.
As shown in Figure 2, the rotary dry distillation furnace 11 comprises a rotary cylinder 11-5 supported by a supporting device 11-9 , the rotary cylinder comprises a front part of the furnace body, a heating section of the rotary furnace body and a discharging end 11-6 connected in sequence; a front part of the furnace shell comprises a feeding end 11-1, an gas outlet 11-2 and a gearing 11-10; the heating section of the rotary furnace body comprises three sections, internal heating tubes 11-8 are arranged along the inside of the three sections, heat source outlets 11-3 are arranged at the front and the middle sections of the heating section respectively, heat source inlets 11-7 are arranged at the middle and the end sections of the heating section respectively; as shown in Figure 3 and Figure 4, an external material-returning device 11-11 and an internal material-returning device 11-12 are arranged in the rotary dry distillation furnace 11.
As shown in Figure 6, the dry distillation heating system 8 which supplies the demanded heat to the rotary distillation furnace 11 comprises a combustion device 8-1, and an air distribution device 8-2 which is connected to the heat source outlets 11-3 and arranged on the combustion device 8-1, and a front end of the combustion device 8-1 communicates with the heat source inlets 11-7 and a tail end of the combustion device 8-1 communicates with an end of the pyrolysis gas fuel; and a tail-end air inlet pipeline of the combustion device 8-1 communicates with a waste-heat recovery device 8-4; the waste-heat recovery device 8-4 is communicated with a fume extractor 8-3 and a combustion-supporting air pipeline respectively; and a hot flue gas circulating device 8-5 is arranged on a air inlet pipeline where the air distribution device 8-2 is connected to the heat source outlets 11-3.
As shown in Figure 5, the cooling device 9, a tubular rotary cooler obliquely installed, comprises a cylinder supported by a supporting device 9-7, heat exchanging tubes 9-4 are arranged inside the cylinder, a cooling shell side 9-3 is formed between an outer wall of the cylinder and the heat exchanging tubes 9-4; a feeding end 9-5 is arranged on a front section of the cylinder, and a discharging end 9-8 is arranged on a tail end of the cylinder which is connected to a cooling medium inlet 9-1 via a rotary joint 9-2 where a cooling medium outlet 9-9 is arranged; a gearing 9-6 is arranged on the cylinder.
The embodiment of the present invention is now described by way of the process of low-temperature dry distillation for oil sand, oil sludge, oil shale and biomass, including the following steps:
1) Raw oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale and biomass (e.g. xylon, straw, solid waste) are crushed and sieved to be with required particle size and are delivered to the stock bin 2 of raw materials by the conveying device 1, materials which is in need of drying and preheating according to water content and technological requirement is measured by the measuring device 3, and then delivered to the drying furnace 14 through a 1#
feeding airlock device 1;
2) The dehydrated and preheated materials is delivered to the surge bin 6 through the 1# discharging airlock device 13, and then is delivered from the surge bin 6 to the rotary dry distillation furnace 11 through the 2# feeding airlock device 7;
materials unnecessarily dehydrated and preheated is delivered directly from the surge bin 6 to the rotary dry distillation furnace 11 through the 2# feeding airlock device 7 after measurement; drying furnace works by means of hot flue gas or steam pipe drying, of which the demanded heat is supplied by the drying furnace heating system which mainly comprises a combustion device, an air distribution device, a dust-extraction device, a fume extractor and a hot flue gas circulating device;
3) The dehydrated and preheated materials is delivered into the rotary dry distillation furnace 11 and moving to a furnace tail along with continuous rotation of . .

the furnace, and is heated and distilled by hot flue gas in an external heating jacket 11-4 and/or the internal heating tubes 11-8 with a sustained reaction time ranging from 30 minutes to 120 minutes, and final reaction temperature of the dehydrated and preheated materials in the rotary dry distillation furnace 11 is ranging from 300 C to 700 C, preferably between 450 C and 650 C, and a pressure value kept in a range of -500 mm H20 to 500 mm H20 by maintaining the micro-positive pressure or the micro-negative pressure in the rotary dry distillation furnace so as to get solid pyrolysis products (e.g. semi-coke, tailings or residue) and pyrolysis gas;
Inert substances with good fluidity (e.g. sand, ceramic ball, ceramic particle or solid pyrolysis products) are added to the raw material which is of high viscosity and poor fluidity so as to reduce the viscidity and improve the fluidity of the raw materials according to following methods:
Method 1: A mixing device is arranged before the rotary dry distillation furnace to mix inert substances of high physical performance and stable chemical property (e.g.
sand, ceramic ball, ceramic particle or solid pyrolysis products) with the raw materials at the weight ratio of 1-2:1, or the solid pyrolysis products are delivered to the mixing device by the conveying device to mix with the raw materials at the weight ratio of 1-2:1, Method 2: The solid pyrolysis products are returned to the feeding end by the internal material-returning device 11-12 or the external material-returning device 11-11 mixing with the raw materials at the weight ratio of 1-2:1 The solid pyrolysis products are returned to the feeding end 11-1 by the internal material-returning device 11-12 or the external material-returning device 11-11 of the furnace body to mix with the raw materials at the weight ratio of 1- 2 : 1 so as to reduce the viscidity and improve the fluidity and the heating rate of the raw materials;

=

the micro-positive pressure or the micro-negative pressure is maintained inside the rotary reactor and the pressure value is kept in a range of -500 mm H20 to 500 mm H20. The produced pyrolysis gas is delivered to the tail gas treatment process to separate and recover its constituents.
The material-returning device is the material-returning screw arranged inside of the furnace 11 with internal material- returning method or the spiral tube or spiral plate set on an outer wall of the furnace body with externally returning material method.
The material at the discharging end of the furnace body automatically returns to the feeding end by the rotation of the furnace without any extra conveying device or conveying power.
The required heat of the rotary dry distillation furnace is supplied by the dry distillation heating system 8 or the external heating jacket or the internal heating tubes. The required heat of the external heating jacket and the internal heating tubes is provided by the dry distillation heating system. The dry distillation heating system is a hot blast system comprising the combustion device, the air distribution device, the fume extractor, the hot flue gas circulating device, the waste-heat utilization device, supporting regulation and control device and the like, in which solid, liquid and gas fuels are burned to generate hot flue gas to supply heat to the furnace.
Fuels and the preheated combustion air burn in the combustion device 8-1 to generate fresh hot flue gas with temperature ranging from 1000 C to 1500 C
which completely mixes with the mid-temperature hot flue gas delivered by the hot flue gas circulating device 8-5 from heat source outlets 11-3 at the ratio of 1 - 8 : 1 in the air-distribution device 8-2 to generate high-temperature hot flue gas with temperature ranging from 600 C to 800 C, and the high-temperature hot flue gas is delivered to the external heating jacket 11-4 or/and the internal heating tubes 11-8 through heat source inlets 11-7 so as to supply heat to the rotary shell 11-5. The mid-temperature of hot flue gas after supplying heat to the rotary shell 11-5 is ranging from 400 C to 600 C, which is delivered from heat source outlets 11-3 to the hot flue gas circulating device 8-5 and then separately delivered to the air distribution device 8-2 and the waste-heat utilization device 8-3. The mid-temperature hot flue gas in the waste-heat utilization device 8-3 transfers heat to the combustion air and becomes low-temperature hot flue gas with a temperature of 180 C or less, and then enters the fume extractor 8-3 after desulfurization and denitrification (desulfurization is not required when the content of sulfur dioxide in flue gas meet the emission standard.) or directly enters the fume extractor to be discharged.
There is provided a dry distillation furnace, an externally-heated rotary furnace installed horizontally and obliquely, of which the shell is supported by supporting device 10-9 and the required power for rotation is from external motivation transferred by gearing 11-10. The produced gas by distillation is discharged from gas outlet 11-2 and is delivered to the pyrolysis gas processing system 12; a plurality of internal heating tubes 11-8 are arranged inside of the rotary shell to supply heat to the material in order to increase heat transfer area and enhance heat transfer efficiency, or internal heating tubes are able to be provided alone without providing external heating jacket additionally. In addition, external material-returning device arranged on the outer wall of the shell or the internal material-returning device 11-12 arranged inside the rotary shell is applied to return the pyrolysis products from the discharging end 11-6 to the feeding end 11-1.
4) The solid pyrolysis products are discharged out of the furnace body through the discharging end 11-6 of the rotary dry distillation furnace, and then is delivered to the cooling device 9 through a 2# discharging airlock device 10, where the products are cooled to 50 C to 120 C, and is finally delivered to the next process or packaged.
The cooling device 9 is a tubular rotary cooler obliquely installed. The solid pyrolysis products discharged out of the rotary dry distillation furnace 11 are delivered into the cooling device 9 through the feeding end 9-5 and then to a shell side of a cooler 9-3, and moving towards the discharging end 9-8 along with the rotation of the shell to be discharged out of the cooler to the next process. The cooling medium is delivered from the cooling medium inlet 9-1 to the heat transfer tubes 9-4 through the rotary joint 9-2 for transferring heat with the solid pyrolysis products from the shell side of the cooler 9-3, and finally is discharged through the cooling medium outlet 9-9;
the rotary cylinder is supported by the supporting device 9-7, of which the required power for rotation is from external motivation transferred by the gearing 9-6.
The cooling medium can be circulating cooling water or desalted water, and the cooling medium is adopted for the following applications:
Method 1. After cooling the material, the medium is delivered to the drying furnace to preheat the raw materials, and then is cooled for circulating use;
Method 2. After exchanging heat, the medium is delivered to the drying furnace for preheating the raw materials, and then to the boiler for generating steam;
Method 3: The medium is directly delivered to the boiler to produce steam.
The cooling methods include direct or indirect cooling or coke quenching by using water, direct or indirect cooling (or coke quenching) by using cold pyrolysis gas, cold inert gas or steam, among which using water to transfer heat indirectly by a tubular rotary cooling furnace is preferable. The cooling of the solid pyrolysis products by the tubular rotary cooler has the advantages of high efficiency of heat transfer, favorable operation environment, and easy recovery and utilization of the heat delivered by the cooling medium.

= CA 02907624 2015-09-21 There is provided a technology that processes raw materials, which includes oil sand, oil sludge (e.g. mixture of crude oil and soil, tank bottom oil sludge, refinery oily sludge), oil shale, biomass (e.g. xylon, straw, solid waste) and their mixture, of particle size ranging from 0 mm to 50 mm, within which a preferable selection is 0 mm to 25 mm.
Detailed description of the invention is illustrated by following embodiments.

Embodiment 1 1) Raw oil sand is crushed and sieved to be with particle size of 6 mm or less, the bulk density of the raw oil sand is 1200 kg/ m3, and its proximate analysis result is shown below:
No. Test Item Result 1 Moisture (Mad) 0.74%
2 Ash Content (Aad) 78.07%
3 Volatile Matter (Vad) 16.33%
4 Fixed Carbon TCad) 5.60 %
2) Raw oil sand is delivered to a raw material storage bin and is measured by a belt scale and through a star unloader, the raw oil sand is delivered to the rotary dry distillation furnace through the surge bin at the speed of 1.2 t/h.
3) The materials delivered to the rotary dry distillation furnace is mixed with 500 C tailings of which the weight is 3 times as the raw materials delivered by an internal material returning screw at the front end of the dry distillation furnace. The mixture flows continuously towards the furnace tail and is heated and dry distilled for 60 minutes by circulating hot flue gas in the external heating jacket at the pressure value of 300 mm H20, finally heated to the temperature of 500 C. Sand tailings, oil from oil sand and pyrolysis gas are produced after distillation. Partial of the sand tailings is discharged from the tail of the rotary dry distillation furnace through the star unloader to a rotary cooling furnace for cooling, and the rest is returned to the furnace head by the internal material-returning screw to mix with raw oil sands at the weight ratio of 2:1 so as to improve the fluidity of the raw materials.
4) The tailings from the discharging end of the rotary dry distillation furnace is delivered to the shell side of the cooler of the tailings and moves towards the discharging end along with the rotation of the cooler shell. Cooling medium, which is circulating cooling water of 31 C, is delivered from the cooling water inlet to the heat transfer tubes through the rotating joint for transferring heat, and is heated up to 37 C
after transferring heat with the tailings in the shell side of the cooler, and then is discharged through a cooling water outlet and recycled after cooled. The tailings in the cooling furnace is cooled to be less than 120 C and delivered to the storage yard of the tailings by the belt conveyor for storage.
The rotary dry distillation furnace is supplied with heat in the following ways:
producer gas from coal-gas producing system burns completely with proper quantity of air which is supplied by air blower and exchanged heat with hot flue gas in the air heat exchanger to produce hot flue gas. The hot flue gas mixes with partial circulated hot flue gas supplied by the high-temperature circulation blower at the tail of the burner, and then enters hot blast pipe, after the adjustment of flap valve at the end of hot blast pipe, hot flue gas enters external heating jacket of the rotary dry distillation furnace to heat the furnace body. The majority of the hot flue gas circulates in the heating system and the rest is discharged after preheating air.
Embodiment 2 1) Raw oil sand is crushed and sieved to be with particle size of 6 mm or less, its proximate analysis result is shown below:

Fischer Assay Ash Fusion Point Proximate Analysis %
C
Oil Mineral High Calorific Specific Content _________________________ Carbon _________________________ Value Weight Moisture Volatile Ash Dioxide Deforma-tion Soften % (Mad) (Vd) (Ad) CO2d % Shale Moi-sture Shale Gas+ kcal/kg Tempe -ing Melting tim3 Oil Semi-coke Loss -rature Tempe Tempe % % %
-11 -rature -rature 1-3 7.83 3.50 17.45 75.41 3.32 6.36 2.96 87.94 2.75 1288 1332 1370 1405 1.9-2.2 P
.
Ash Component "
Heat Intensity, >25mm,%
.
ok , Average Specific "
Heat Heat N) Heat Intensity Intensity of Raw Shale Intensity of kcal/kg. C
r.t Na20, 'S
of Ash Si02 A1203 Fe2O3 CaO MgO
of Temperature Semi-coke K20, etc 7 550 C,2 82.5 79.7 41.7 0.24 60.8-62.9 21.6-30.5 5.3-11.6 0.66-1.6 1.1-2.0 0.65 2) Raw oil shale is delivered to a raw material storage bin by a belt and is measured by a belt scale, and then to a steam-pipe drying furnace through a star unloader at the speed of 4.2 t/h for preheating the raw material to 100 C with less than 0.5% moisture content, continuously moves towards the furnace tail as the shell rotates, and is finally discharged from the furnace body through a discharge bin of the furnace tail. The dust within the dry tail gas is separated and collected by a first-level cyclone separator and a first-level bag-type dust collector.
3) The dehydrated and preheated oil shale is delivered from a star unloader to the rotary dry distillation furnace through a slide pipe, continuously flows towards a furnace tail as the furnace body rotates, and is heated and dry distilled for 90 minutes by circulating hot flue gas in the external heating jacket, at a pressure value of 200 mm H20, finally to 550 C for thermal cracking so as to produce shale semi-coke and high-temperature gas mixture of shale oil and pyrolysis gas, and then the gas mixture is delivered to an oil-vapor recovery system for separating and recycling oil shale and pyrolysis gas.
The analysis result of shale semi-coke is shown below:
Calorific Mad, % Aad, % Vad, % FCad,13/0 Value, Kcal/kg 0.03 81.4 9.07 9.5 538 The analysis result of shale oil is shown below:

Item Result Specific Weight g/cm3 0.90..
Tar Acid %(volume) 3.7 Tar Base %(volume) 2.5 Kinematic Viscosity cp (centipoises) 10.3 Freezing Point C 33 Paraffin Content 20.2 Asphaltene 0.85 Colloid Content 0/0 42 (Sulfuric Acid Method) Initial Boiling Point C 216

10% Distillation Temperature C 264 20% Distillation Temperature C 293 Distillation Range 30% Distillation Temperature C 318 40% Distillation Temperature C 343 50% Distillation Temperature C 362 % 85.39 12.09 % 0.54 Element Composition N % 1.27 0 % 0.71 C/H % 7.06 Characteristic Factor 11.52 The analysis result of pyrolysis gas is shown below:
Main Components of Pyrolysis Gas w%
CO2 CnHm CO H2 C0H20+2 61.37 7.80 6.84 4.86 19.12 4) The shale semi-coke from a discharging end of a rotary dry distillation furnace is delivered to the shell side of the cooler and moves towards the discharging end as the cylinder of the cooler rotates. Cooling medium, which is desalted water of 25 C, is delivered from a cooling water inlet to heat transfer tubes through a rotating joint for transferring heat with the semi-coke in the shell side of the cooler and is heated up to be 70 C, and is discharged through a cooling water outlet to a gas-fired boiler so as to supply steam to the steam pipe drying furnace. The shale semi-coke is cooled to be less than 80 C in the cooling furnace and then delivered to the semi-coke storage yard by a belt conveyor.
The rotary dry distillation furnace is supplied with heat in the following ways:
heavy oil completely burns with proper quantity of preheated air in proportion to produce hot flue gas. The hot flue gas mixes with partial circulated hot flue gas supplied by the high-temperature circulation blower at the tail of the burner, and then enters hot blast pipe, after the adjustment of flap valve at the end of hot blast pipe, hot flue gas enters an external heating jacket of the rotary dry distillation furnace to supply heat for the furnace body. The majority of the hot flue gas circulates in the heating system and the rest is discharged after preheating air. Pyrolysis gas is delivered to a gas fired boiler to generate steam for steam pipe drying furnace.
Embodiment 3 1) Sieved and tattered raw sawdust is briquetted to be with particle size of 6 mm or less by a impact briquetting machine, whose main performance indexes are shown below:
Forming density: 1.4 t/m3 Moisture content: 14%
Calorific value: 14 MJ/kg 2) Sawdust briquettes are delivered to a raw material storage bin by a belt and are measured by a belt scale, and then are delivered to a rotary drying furnace through a star unloader at the speed of 0.8 t/h. The raw material is rotating with the rotation of the drying furnace and lifted up by lifting plate installed inside of the drying furnace, and then dropping down evenly, during its dropping the material fully contacts with hot flue gas from a combustion furnace so as to preheat the material to 80 C to remove the moisture within and the gas absorbed in the pores of sawdust briquettes, and then the material moves towards to a tail of the furnace with rotation of a cylinder and finally discharged out of a furnace through a discharging bin of the furnace tail. Small amount of dust within a dry tail gas is separated and collected by a first-level gravity dust separator and a first-level bag-type dust collector.
3) The dehydrated and preheated sawdust briquettes are delivered from a star unloader to the rotary dry distillation furnace through an slide pipe , continuously flow towards a furnace tail as a furnace body rotates, and are heated and dry distilled for 60 minutes by circulating hot flue gas in an external heating jacket and internal heating tubes, at a pressure value of 500 mm H20, finally to 550 C for thermal cracking so as to generate charcoal, and high-temperature gas mixture of wood tar, wood vinegar and pyrolysis gas, the gas mixture is delivered to an oil-vapor recovery system for separating and recycling wood tar, wood vinegar and pyrolysis gas.
Calorific value of charcoal: 3600 kcal/kg Moisture content of wood tar: 10%
Acetic acid content of wood vinegar: 69%
Components of pyrolysis gas:
Main Components of Pyrolysis Gas, Calorific Density vol% Value kg/m3 28.1 23.6 0.7 0.4 0.5 1.3 0.7 2.0 26.0 18.6 1.0 17.4 4) The charcoal from a discharging end of the rotary dry distillation furnace is delivered to the shell side of the cooler of the charcoal, moves towards the discharging end as the cylinder of the cooler rotates. Cooling medium, which is circulating cooling water of 31 C , is delivered from a cooling water inlet to heat transfer tubes through a rotating joint for transferring heat with the tailings in the shell side of the cooler to be heated up to 37 C, is discharged through a cooling water outlet and recycled after being cooled. The charcoal in the cooling furnace is cooled to be less than 60D and is delivered to the charcoal packaging process by a belt conveyor.
The rotary dry distillation furnace is supplied with heat in the following ways:
heavy oil completely burns with proper quantity of air which is supplied by air blower and exchanged heat with hot flue gas in the air heat exchanger to produce hot flue gas. The hot flue gas mixes with partial circulated hot flue gas supplied by the high-temperature circulation blower at the tail of the burner, and then enters hot blast pipe, after the adjustment of flap valve at the end of hot blast pipe, hot flue gas enters external a heating jacket of the rotary dry distillation furnace to supply heat for the furnace body. 75% of the hot flue gas circulates in the heating system and the rest is discharged after preheating air. Hot flue gas produced by the combustion of pyrolysis gas supplies heat for the drying furnace.
Embodiment 4 1) Raw oil sand is crushed and sieved to be with particle size of 6 mm or less, its proximate analysis result is consistent with that of the embodiment 1.
2) Raw oil sand is delivered to a raw material storage bin by a belt and is measured by a belt scale, and then to a rotary drying furnace through a star unloader at a the speed of 4.2 t/h. The raw material is rotating with the rotation of the furnace and lifted up by lifting plate installed inside of the drying furnace, and then dropping down evenly, during its dropping the material fully contacts with hot flue gas from combustion furnace so as to preheat the material to 100 C to remove the moisture within and gas absorbed in the pores of oil sand, and then the material moves towards to a tail of the furnace with rotation of a cylinder and finally discharged out of the furnace through a discharging bin of the furnace tail. Dust within the dry tail gas is separated and collected by a first-level gravity dust separator, a first-level bag-type dust collector and a first-level electrostatic dust collector.
3) The dehydrated and preheated oil shale is delivered from a star unloader to the rotary dry distillation furnace through a slide pipe, mixes with dry river sand (using river sand at the initial stage, using tailings instead after tailings is produced in the dry distillation furnace,) to improve the fluidity, continuously flows towards a furnace tail, and is heated and dry distilled for 60 minutes by circulating hot flue gas in an external heating jacket, at a pressure value of -500 mm H20, finally to 500 C for thermal cracking so as to generate tailings, oil from oil sand and pyrolysis gas.
4) The tailings from a discharging end of the rotary dry distillation furnace is delivered to a water-sealing discharge bin where the tailings directly contacts water and is cooled to be less than 50 C with moisture content within 20%, taken out from water by a scraper conveyer, and delivered to a storage yard of tailings by a belt conveyer.
Pyrolysis gas is delivered to a drying furnace heating system to generate hot flue gas for the drying furnace.
Embodiment 5 1) Raw oil sand is crushed and sieved to be with particle size of 6 mm or less and the bulk density of the raw oil sand is 1200 kg/ m3, and its proximate analysis result is shown below:
No. Test Item Result 1 Moisture Mad 0.74%
2 Ash Aad 78.07%
3 Volatile Vad 16.33%
4 Fixed Carbon FCad 5.60%
2) Raw oil sand is delivered to a raw material storage bin by a belt and is measured by a belt scale, and to an externally-heated drying furnace through a star discharge bin at the speed of 4.2 t/h. The raw materials is preheated to 50 C
by the =
medium of demineralized water of 70 C from a cooling furnace, continuously moves towards a furnace tail with the rotation of a cylinder, and then is discharged from a preheating furnace body through a discharge bin of the furnace tail.
3) The preheated oil sand is delivered from a star unloader to the rotary dry distillation furnace through a slide pipe , continuously flows towards the furnace tail as a furnace body rotates, and is heated and dry distilled for 90 minutes by circulating hot flue gas in an external heating jacket, at a pressure value of 300 mm H20, finally to 500 C for thermal cracking so as to generate tailings, oil from oil sand and pyrolysis gas which is delivered to an oil-vapor recovery system for separating and recycling oil from oil sand and pyrolysis gas.
4) The tailings from a discharging end of the rotary dry distillation furnace is delivered to the shell side of the cooler the tailings and moves towards the discharging end with the rotation of the cooler shell. Cooling medium, which is demineralized water of 25 C, is delivered from the cooling water inlet to heat transfer tubes through a rotating joint, the temperature of the cooling medium is heated up to 70 C after transferring heat with the tailings in the shell side of the cooler, and then is discharged through a cooling water outlet to an external preheating furnace for preheating raw oil sand, and then the temperature reduces to be less than 100 C and delivered to the storage yard of the tailings by a belt conveyor for storage.
The rotary dry distillation furnace is supplied with heat in the following ways:
producer gas from coal-gas producing system burns completely with proper quantity of air which is supplied by air blower and exchanged heat with hot flue gas in the air heat exchanger to produce hot flue gas. The hot flue gas mixes with partial circulated hot flue gas supplied by the high-temperature circulation blower at the tail of the burner, and then enters hot blast pipe, after the adjustment of flap valve at the end of hot blast pipe, hot flue gas enters an external heating jacket of the rotary dry distillation furnace to supply heat for the furnace body. The majority of the hot flue gas circulates in the heating system and the rest is discharged after preheating air.
Embodiment 6 1) Oily sludge, mixture of crude oil and soil of viscous solid in paste shape, is adopted, whose analysis result is shown below:
No. Test Item Unit Result 1 Moisture (Mad) 19.96 2 Ash (Ad) 2.15 3 Volatile (Vdaf) 96.17 4 Fixed Carbon (FCad) 3.00 5 Char Residue Characteristics (CRC) 1-8 2 6 Total Sulfur (dry basis) (St,d) 0.45 Carbon (dry basis) (Cd) 74.20 7 Element Anal ysis Hydrogen (dry basis) (Hd) 14.12 Nitrogen (dry basis) (Nd) 0.47 Oxygen (dry basis) (Od) 8.61 Yield of Total Water(Water,ad) 16.50 Gray-King Yield of Tar (Tar,ad) 82.30 8 Low-temperature Dry Yield of Semi-coke (CRad) 0.70 Distillation Coal Gas+Loss 0.50 The raw oil sludge completely mixes with tailings (using sand, ceramic ball, ceramic particle or solid pyrolysis products with particle size of 8 mm or less at the stage of furnace start-up without tailings) in a mixing device at the weight ratio of 1:2 so as to form loose mixed materials.
2) Mixed materials is delivered to a raw material storage bin by a belt and is measured by a belt scale, and then to an externally-heated drying furnace through a star unloader at the speed of 2.4 t/h for dehydrating the water content to be 5% or less and heating up to 80 C by using steam as the medium, and then continuously move towards a furnace tail as the cylinder rotates, and is finally discharged from the preheating furnace body through the discharge bin at the furnace tail.
3) The preheated mixed materials is delivered from a star unloader to the rotary dry distillation furnace through a slide pipe , continuously flows towards a furnace tail as a furnace body rotates, and is heated and dry distilled for 60 minutes by circulating hot flue gas in an external heating jacket, at a pressure value of 200 mm H20, finally heated to 550 C for thermal cracking so as to produce tailings, pyrolysis oil and pyrolysis gas which is delivered to an oil-vapor recovery system for separating and recycling pyrolysis oil and pyrolysis gas.
4) The tailings from a discharging end of the rotary dry distillation furnace is delivered to the shell side of the cooler of the tailings, moves towards the discharging end as the cylinder of the cooler rotates. Cooling medium which is demineralized water of 25 C is delivered from a cooling water inlet to heat transfer tubes through a rotating joint for transferring heat with the tailings in the shell side of the cooler to be heated up to 37 C, is discharged via a cooling water outlet and delivered to an air cooler for cooling, and then recycles for using. Partial of the tailings which is cooled to be less than 80 C is delivered to a mixing device by a belt conveyer, and the rest is to the storage yard.
The rotary dry distillation furnace is heated by same method as that of the embodiment 5.
It shall be noted that the foregoing description represents the preferable embodiments of the present invention, and is intended to illustrate and not limit the scope of the invention. While the invention has been described hereinabove in detail in conjunction with the embodiment, those skilled in the art can modify the technical solutions or make equal substitutions in technical features of the embodiments.
All modifications, substitutions or improvements, made by those ordinarily skilled in the art without departing from the spirit and scope of the present invention, are intended to be included within the scope of the invention.

Claims

1. An apparatus for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass, which comprises a conveying device (1), a stock bin (2) connected to the conveying device (1), and a metering device (3) connected to the stock bin (2), wherein the metering device (3) is connected to a drying furnace (14) and a surge bin (6) respectively, the metering device (3) is connected to the drying furnace (14) via a 1# feeding airlock device (4), the drying furnace (14) is connected to the surge bin (6) via a 1# discharging airlock device (13); and the surge bin (6) is connected to a rotary dry distillation furnace (11) and a cooling device (9) in sequence, the surge bin (6) is connected to the rotary dry distillation furnace (11) via a 2# feeding airlock device (7), the rotary dry distillation furnace (11) is connected to the cooling device (9) via a 2# discharging airlock device (10).

2. An apparatus for low temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 1, wherein the rotary dry distillation furnace (11) is connected to a pyrolysis gas processing system (12) and a dry distillation heating system (8) respectively.

3. An apparatus for low temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 1, wherein the rotary dry distillation furnace (11) comprises a rotary cylinder (11-5) which is supported by a supporting device (11-9), and the rotary cylinder (11-5) comprises a front part of the furnace body, a heating section of the rotary furnace body and a discharging end (11-6) connected in sequence; the front part of the furnace body is provided with a feeding end (11-1), a gas outlet (11-2) and a gearing (11-10);
the heating section of the rotary furnace body comprises three sections, internal heating tubes (11-8) are arranged along the inside of the three sections, heat source outlets (11-3) are arranged at a front section and a middle section of the heating section respectively, heat source inlets (11-7) are arranged at the middle section and an end section of the heating section respectively; and the rotary dry distillation furnace (11) is provided with an external material-returning device (11-11) and an internal material-returning device (11-12).

4. An apparatus for low temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 1, wherein the dry distillation heating system (8) comprises a combustion device (8-1) and an air distribution device (8-2) connected to the heat source outlets (11-3) and arranged on the combustion device (8-1); a front end of the combustion device (8-1) communicates with the heat source inlets (11-7) and a tail end of the combustion device (8-1) communicates with an end of the pyrolysis gas fuel;
a tail-end air inlet pipeline of the combustion device (8-1) communicates with a waste-heat recovery device (8-4), the waste-heat recovery device is communicated with a fume extractor (8-3) and a combustion-supporting air pipeline respectively; and a hot flue gas circulating device (8-5) is arranged on an air inlet pipeline which connects the air distribution device (8-2) and the heat source outlets (11-3).

5. An apparatus for low temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 1, wherein the cooling device (9) comprises a cylinder supported by a supporting device (9-7), heat exchanging tubes (9-4) are arranged inside the cylinder, a cooling shell side (9-3) is formed between an outer wall of the shell and the heat exchanging tubes (9-4); a feeding end (9-5) is arranged at a front end of the cylinder and a discharging end (9-8) is arranged at a tail end of the cylinder, the discharging end (9-8) is connected to a cooling medium inlet (9-1) via a rotary joint (9-2) where a cooling medium outlet (9-9) is arranged; a gearing (9-6) is arranged on the cylinder.

6. A process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass, wherein the process comprises the following steps:
1) raw oil sand, oil sludge, oil shale or biomass is crushed and sieved to the required particle size and delivered to a raw materials stock bin by a conveying device (1) , and then to a drying furnace (14) through a 1# feeding airlock device (4) after the measurement by a metering device (3);
2) the dehydrated and preheated raw materials are delivered to a surge bin (6) through a 1# discharging airlock device (13), and then to a rotary dry distillation furnace (11) through a 2# feeding airlock device (7);
3) the materials in the rotary dry distillation furnace (11) are heated and dry distilled by hot flue gas in an external heating jacket (11-4) or/and internal heating tubes (11-8); a mixing device or a material-returning device is provided for dry distillation before the rotary dry distillation furnace (11) if the raw material is of high viscosity and poor fluidity; certain temperature and micro-positive pressure or micro-negative pressure is maintained inside the rotary dry distillation furnace (11) and the produced hot pyrolysis gas is sent to a tail gas treatment process to separate and recycle the components thereof; and 4) the solid pyrolysis products are discharged out of a furnace body through a discharging end of the rotary dry distillation furnace (11), and are delivered through a 2# discharging airlock device (10) and to a cooling device (9) via a feeding end (9-5), and then to a shell side of a cooler (9-3), after that the solid pyrolysis products are delivered to next process or packaged to product after cooling.

7. A process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 6, wherein the raw materials unnecessarily dehydrated and preheated are directly delivered from the surge bin (6) to the rotary dry distillation furnace (11) through the feeding airlock device after measurement.

8. A process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 6, wherein, in the step 3, the reaction time of the materials in the rotary dry distillation furnace is ranging from 30 minutes to minutes, final reaction temperature is ranging from 300 °C to 700 °C , and micro-positive or micro-negative pressure is maintained and pressure value is ranging from -500 mm H2O to 500 mm H2O in the rotary dry distillation furnace.

9. A process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 6, wherein, in the step 3, a mixing device is arranged before the rotary dry distillation furnace (11) to mix sand, ceramic ball, ceramic particle or solid pyrolysis products with the raw materials at the weight ratio of 1-2:1;
or solid pyrolysis products are delivered to the mixing device by a conveying device and mixed with the raw material at the weight ratio of 1-2:1.

10. A process for low-temperature dry distillation of oil sand, oil sludge, oil shale and biomass according to claim 6, wherein, in the step 3, the material-returning device is provided for dry distillation, solid pyrolysis products are returned to a feeding end by an internal material-returning device (11-12) of a furnace body of the rotary dry distillation furnace 11 or an external material-returning device (11-11) of the furnace body to mix with the raw material at the weight ratio of 1-2:1.