JPS5819385A - Method and apparatus for recovering oil and gas from oil shale - Google Patents

Abstract

PURPOSE:To efficiently recover oil from oil shale, by crushing the oil shale, adjusting its particle size and then recovering heat in a plurality of zones in which fluidized layers are formed. CONSTITUTION:In a drying zone A, an oil shale layer 2 is formed by loading a movable grate 1 with crushed oil shale. The layer 2 first enters the drying zone A as the movable grate 1 moves, and is exposed to a hot gas stream produced by burning part of a dry distillation product gas generated in a dry distillation zone B and supplied through a line 17, and dried by vaporizing part of adhering water and water of crystallization of the oil shale. The oil shale layer 2 subjected to dry distillation in the dry distillation zone B is supplied into a crusher C and, after crushed into a necessary particle size, supplied into a combustion tower D. The solid particle is kept being fluidized by an oxygen-contg. gas introduced through a line 15 and a combustible component is burned. The exhaust gas is discharged from the top of the combustion tower through a line 16 and introduced into the bottom of the furnace F.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for recovering oil and gas from oil shale and the construction of an apparatus for use in this method. More specifically, there is a moving grid, and a fixed wind box is installed under the ground of the moving grid, and there is water between the wind box and the moving grid, so that the gas inside the wind box is released outside. lc
A device with a structure that prevents spillage (hereinafter referred to as a moving lattice device) is used, and the moving lattice device is divided into one section or two sections. After drying and carbonizing oil shale, the oil shale is pulverized in a pulverization section to adjust the particle size, and the amount of heat held by the oil shale is efficiently recovered in multiple sections forming a fluidized bed state. The present invention relates to a method and apparatus for efficiently recovering oil from oil shale.

The object of the present invention is to provide a movable grid type device which eliminates the drawbacks of the prior art.
Using a device that combines a crushing device and a fluidized bed device.
It is an object of the present invention to provide a method for recovering oil from oil shale. (1) Carbonization of oil shale can be achieved without changing the operating conditions of a moving grid type device even if the water content in the raw oil shale changes. (2) To facilitate the operation of the fluidized bed type fuel flIi tower by crushing the oil shale lumps carbonized in the moving grid type device and adjusting the particle size; (3) By reducing the solid particle size of oil shale, combustion in a fluidized bed combustion tower becomes easier.
(4) Improving the thermal efficiency of oil shale carbonization plants; (4) Improving the thermal efficiency of oil shale carbonization plants; (Excellent) Utilizing low-grade heat such as waste heat of combustion exhaust gas. It is possible to produce carbonized gas with a high calorific value. (1) (2) (3) (5) (
6) can be achieved. In other words, the purpose is to provide an economical oil shale drying plant.

Regarding the method of carbonization of oil shale using a moving lattice type device, please refer to the patent application No. 1983-2003. No. 0820, and a method and apparatus for drying oil-containing minerals using a fluidized bed was published by KII in the publication dated June 26, 1982 (title of invention: method and apparatus for carbonizing oil-containing minerals). However, by combining these methods, we propose a new technology for carbonizing oil shale even more efficiently.

Oil shale differs in its thermal decomposition characteristics, but the amount of adhering moisture is 3 to 10 degrees, and the amount of crystallized water is 1 degree.
Contains ~4 vt-seismic intensity. When the oil shale is preheated and dried to emit this adhering water and crystal water, JIK 11 of the oil shale is generated and becomes an unusually small amount of II&.

Oil shale should be carbonized, I! Approximately half of the hydrocarbon compounds contained in Fs are released as carbonized oil and gas, but dry l111O oil shale contains the highest amount of effective acids, mainly carbonaceous (C). @Half of it is pickled even once. Therefore, as a method of adding H to this effective carbonaceous material, as proposed in the previous patent application, the method is to burn Zengji carbon trade with oxygen-containing gas).
There is a way to translate it as il energy.

In this case, in the carbonaceous combustion process in the oil shale solid particles, the reaction gradually progresses from the surrounding particles toward the inside. This combustion reaction rate is fast on the surface of the solid particle, but as the reaction progresses inside, the rate at which oxygen diffuses into the solid particle becomes slower, so the combustion reaction rate also becomes slower. Therefore, the smaller the solid particle diameter is, the faster the above-mentioned oxygen diffusion rate *-ex is, so the combustion rate is also faster, and as a result, the carbonaceous thermal energy recovery efficiency becomes higher. That is, the literature (PLG, Mallonate,.

Quarterly of th@coloraclo
5chool of Min・471 (4) 30
? (1974)) According to K., when 75 grain size O oil shale (Colorado meaning) are combusted at 538°C KTh, with 114 Kg/wl of gas supplied, 30 vtll GO carbon is produced. 3 to burn
It's also time consuming. On the other hand, if the particle size is 1O-1i
If the combustion time is reduced by a certain degree, the combustion time will be reduced by a certain degree in the above conditions. Therefore, the device shape can also be made smaller.

Therefore, in terms of shortening the time required for the combustion process and increasing thermal energy recovery efficiency,
Inventions with dated patent applications are more advantageous.

However, a lot of power is required to crush the raw oil shale into small particle sizes before supplying it to the preheating and drying process 11. If the cracked lumps are crushed into smaller particles during the preheating, drying, and carbonization steps, the power required will be reduced.

The bulk size of the oil shale raw material to be supplied to the moving grid type device is large particle size, and 100-11 degrees is used. On the other hand, the particle length for forming a fluidized bed is generally KO,
Oil shale having a temperature of 1 to 1 (+-111 degrees Celsius) is used. Also, part of the oil shale is crushed during the drying and carbonization process, resulting in a reduction in particle size.

Therefore, the amount of work is calculated for the case where 100 mm of oil shale raw material is crushed to a small particle size of 10 mm, and when the particles crushed to 50 or 30 mφ in the drying and carbonization process are further crushed to 10 mm. The comparison is as follows.

Here, the 1ck equation (Chemical Engineering Handbook, Maruzen Co., Ltd., 1271 r1978) was used as the equation regarding the amount of work WK.

W klog (to DI) Where, W: Work amount [''kvhr/l] k: Constant [hvhr/z] D1* DI ``Particle size [-], As seen in this table, oil shale raw material chunks of 10
The amount of work (Na2 or N113) required to crush the oil shale chunks crushed in the drying/carbonization process into 10 mm is approximately 50 to 70 mm, compared to the amount of work W(Ial)K required to crush 0 mm to 10 mm. become.

Therefore, the method and apparatus according to the present invention can significantly reduce the amount of work compared to conventional methods.

Moreover, the thermal energy utilization efficiency during the time required for the preheating, drying, and carbonization steps is not much different from that in the case of utilizing the invention of the above-mentioned patent application filed on June 26, 1980.

Therefore, as proposed in the present invention, lI
K oil shale lumps are pulverized by a crusher, transported to a crusher, and the particle size is reduced and the particle size is adjusted to the average level.If this is combined with the combustion and cooling processes that utilize a fluidized bed, both threats will be achieved. It has been found that a preferable drying method that combines the following advantages can be obtained.

The pulverized particle size varies depending on the physical properties of the oil shale, but
．． A range of 1 to 10°C is preferable for forming a fluidized bed state.

Next, an example of the actual i*ms of the present invention will be explained with reference to the accompanying drawings.

1 shows a system diagram of an embodiment of the present invention that combines a moving grating arm called a JIIN II, a dP grating, a straight grate, etc., a crushing and sizing device, a fluidized bed type device, and a heating furnace.

The oil shale layer 2 loaded on the moving grid 1 is moved through the drying zone A1 divided by the partition walls I and y and the carbonization zone B divided by the partition walls y and 2, and is exposed to the gas flow supplied to each zone. It is preheated, dried and carbonized.

That is, in FIG. 1, on the left side of the drying zone A, oil shale crushed material is loaded onto the moving grid 1 using an oil shale supply device (not shown), and the entire oil shale layer 2 is blown away. As the moving grid 10 moves, it first enters the drying section A, and some of the carbonized gas generated in the carbonized section B is transferred to the heating furnace. The oil quencher is exposed to the hot gas RtIC obtained by combustion and supplied through line 17 to evaporate and dry part of the water and crystallized water adhering to the oil quencher.

The oil shale layer 2 to be dried is moved to the drying section IIB, where a part of the carbonized product gas obtained by cooling and separating the carbonized product generated in the carbonized section B is heated with a heating FF. 1? It is carbonized by being exposed to a heated gas stream supplied by the plant.

The gas that flows out of the drying section A through line 3 contains a large amount of water, so after separating and removing the water in the gas-liquid separator G, the gas passes through Proa E and flows out from line 4, and the separated water flows through line S. It is discharged outside the system.

The gas that has flowed out of carbonization zone B via line 6 is transferred to Oil Quencher-JS Heat Exchanger II in order to entrain the carbonization products.
After passing through IK, it is separated into produced gas and produced oil in a gas-liquid separator, and the produced oil passes through line 7, and a part of it is circulated and used as quencher JO@@oil via circulation pump V. It is extracted out of the system through line 8 as lumbar oil.

-The generated gas separated by the gas-liquid separator is drawn to the blower M, and a portion is supplied to the cooling tower (line 10) as cooling gas, and a portion is transferred to the line 10. ] The remaining gas is supplied as a fuel gas to line 11 as a product gas.
exposed outside the system.

The oil shale layer 2 carbonized in the carbonization section B is fed into the crusher C, where it is crushed into a particle size necessary to form a fluidized bed in the next combustion tower. It is then supplied to the middle lower part of the combustion tower. The solid particles of oil shale supplied to the combustion tower are held in the fluidized bed by the oxygen-containing gas fed through line 15 from the combustion JFDT section, and the carbonaceous gold particles in the solid particles are The combustible matter to be collected is burned, and the exhaust gas is discharged from the combustion tower soil section through a 2-in-16 tube and sent to the heating furnace. Below @Ic is sent.

The oxygen-containing gas sent from line 15 to the combustion tower DK is drawn from line 12 to Proa P, preheated in a heat exchanger, and passed through line 15 to the heating furnace. Indirectly heated gas (twin 14) is used. A part of the neck gas passes through the line holder and is used as combustion air in the heating furnace F.

The particles of fireflies that burned the combustible matter Ia in the combustion tower are transferred to the middle lower part of the cooling tower E mainly by their own weight through the middle upper part 11C of the combustion tower The cooling gas (this
In this case, the carbonization product gas -II) K forms a fluidized bed state, and the sensible heat held by the integral particles is transferred to the cooling gas Kf.
After being cooled to about 100 to 150 degrees Celsius, it is discharged from the middle upper part of the system through the line -1 as a waste product.

In the heating FF, the amount of heat generated by burning a part of the carbonized product gas supplied from the line 10 is transmitted to the exhaust gas discharged from the upper part of the cooling tower 1 via the line 18,
The cooling tower exhaust gas heated to a high temperature is supplied through line 19 as heating gas to Zengji Qianxu District B. In this way, as the axillary cooling gas (heating gas in the carbonization zone 11m), it is possible to use a part of the carbonization product gas W*1ltL.

As mentioned above, this method involves circulating and using the carbonized product gas without oxygen as the heating gas in the carbonization zone B, rounding in which the product gas and product oil do not burn, and highly crystalline product gas and Luminous oil can be diluted with lI.

Optimal temperature range I for each section! Although it varies depending on the physical properties of IFi oil shale, the drying section A shown in the method shown in Figure 1
is about 100-350℃ (preferably 100-150℃1
1 degree), carbonization section B~900℃ (preferably F1
550-750'C11 degree), combustion tower 500-11
00°C (preferably 700-900°C), cooling 4 times 1
About 00 to 200°C and 0iltI[B are preferable.

The oxygen-containing gas fed into the combustion tower may be pure oxygen gas, but generally 9 gas is used as described above. Further, the combustion exhaust gas containing residual fluorine may also be used for circulation.

In the embodiment shown in FIG. 1, the crushing device C is shown connected to the movable grate device and the combustion tower, but the movable grate device or the combustion tower! 4D is better with a separate device. When these devices are connected, solid particles can be treated at high temperatures, so no heat is released, resulting in a device with high thermal efficiency.

On the other hand, in the case of the connected nine structure, the crushing device C must be able to withstand high temperatures, but if it is a separate device, low-temperature processing becomes possible.

The crushing process C not only crushes oil shale lumps into small particles a, but also crushes the crushed solid particles to form a fluidized bed in the next combustion 111$D. It is preferable to use one that also has the function of classifying into particle groups.

As explained above, in the method of the present invention, gas heated by an indirect heater, that is, high-grade heat, is used only for carbonization of hydrocarbon compounds, which is the original purpose of oil shale drying, and the attached moisture is removed. Low-grade heat such as combustion exhaust gas is used to preheat and dry oil shale, which requires a large amount of heat when the quantity is poor. It is easy to understand that the amount of heat can be efficiently recovered by MKL during smoke, and Honjitsu WR is a method of recovering oil from excellent oil shale.

Regarding the structure of the layout, the joint positions of piping, etc. shown in Figure 1 used to explain the above embodiments, please refer to Figure 1 of Zeng.
There is no ID restriction, and it may be anything that does not deviate from the idea of the present invention.

[Brief explanation of the drawing]

FIG. 1 is an explanatory diagram showing an example of an embodiment of the present invention. Sub-Agents 1) Meifuku Agent Ryo Uta Gan - Continued from page 1 0 Author: Kou Otawa, 4-6-22 Kannon Shinmachi, Nishi-ku, Hiroshima City, Mitsubishi Heavy Industries, Ltd., Hiroshima Shipyard 0 Author: Keizo Arai Mitsubishi Heavy Industries, Ltd. Hiroshima Shipyard, 4-6-22 Kannon-Shinmachi, Nishi-ku, Hiroshima August-8, 1980 Haruki Shimada, Commissioner of the Japan Patent Office 1, Indication of the Case 1982 Patent Application No. 116361 Related patent applicant address: 2-5-1-4 Marunouchi, Chiyoda-ku, Tokyo;
Agent address: 24 Toranomon-chome, Minato-ku, Tokyo @ No. 11 Subject of correction <d[IIor 41f? lJ seeking o1 [! [J 01
[(2) Specification Or Detailed Explanation of the Invention - JO Section & Amendment O Contents [) % Allowance Claim 0III on the first page of the specification! Another 1m away!
Correct as in (). (2) Specification number! On the 7th line of the page, correct "or set" to "for this". Claims (1) In recovering oil and combustible gas by thermally decomposing oil shale, first a layer of oil shale agglomerates consisting of coarse particles is formed on a horizontal surface, and the layer is continuously moved horizontally. A preheated drying gas is passed through the layer in the first section while the granules are heated at a temperature of 100 to 550°C within a range where substantial carbonization of the hydrocarbon compounds contained in the granules does not occur. After preheating and drying, the layer is moved to a second section where carbonization is carried out, where non-oxidizing high temperature heated gas is passed through to remove the particles contained in the granules preheated and dried in the first section. Carbonate the hydrocarbon compounds, cool the carbonized product,
Oil and combustible gas are recovered by gas-liquid separation, and the remaining granules with different particle sizes are pulverized and adjusted to the particle size necessary to maintain a fluidized bed state. The body is transferred to the subsequent combustion process, where a fluidized bed is formed by a flow of oxygen-containing gas, and the combustibles that could not be thermally decomposed in the carbonization process are burned and the heat is recovered. The waste solids are transferred to a cooling process to form a fluidized bed state by a cooling gas flow, and the sensible heat held by the residual powder and granules is transferred to the cooling gas, and the cooled waste solids are discharged from the system and discharged from the cooling process. A method for recovering oil and gas from oil shale, which is characterized by recovering heat from the gas as well. (2) A wind box is provided, which is divided by a moving grid installed horizontally and configured to be able to move continuously in one direction along the surface thereof, and two partition walls that cross the moving grid, one of which has preheating, A dry gas inlet and a dry exhaust gas outlet on the other side, an oil shale supply port on the upper part of the moving grid of the partition wall a on the upstream side with respect to the moving direction of the partition walls, and a preheating part on the upper part of the moving grid of the partition wall A on the downstream side. , a drying section A comprising a dried granule outlet, and a wind box divided by the partition wall and a partition wall C downstream thereof, one of which has a heating gas inlet and the other side a carbonization product outlet. , a movable grid type apparatus having a carbonization section B having a residual granule outlet on the upper part of the movable grid of the partition wall C, and a crushing apparatus having a residual granule inlet on one side and a granule outlet on the other side; A granule inlet opens at the middle lower part of the fluidized bed formed inside, a residual powder outlet at the middle upper part of the fluidized bed, a gas inlet containing oxygen at the lower part, and an oxygen-containing gas inlet at the upper part. consists of a combustion tower equipped with a combustion gas outlet, a high-temperature residual powder inlet in the middle lower part of the fluidized bed formed inside, and a cooled waste solids outlet in the middle upper part of the fluidized bed. A cooling tower comprising a cooling gas inlet at the bottom and a cooling exhaust gas outlet at the top, a cooling separation device and carbonization product gas each having a carbonization product inlet on one side, a carbonization product gas outlet and a carbonization product oil outlet on the other side. A heating furnace is installed in parallel to burn part of the gas, and to heat another part of the carbonized gas by indirect heat exchange.
The residual granule outlet of the mobile grating device, the residual granule inlet of the crusher, the powder outlet of the crusher, the powder inlet of the combustion tower, the residual powder outlet of the combustion tower, and the residual powder of the cooling tower. The granule inlets are connected to each other via downcomers, and the carbonization product outlet of the carbonization section B is connected to the carbonization product inlet of the cooling and separation device, and the carbonization product gas heated in the heating furnace is An apparatus for recovering oil and gas from oil shale, characterized in that the inlet of the carbonization section B is connected to the inlet of the drying section A, and the combustion exhaust gas of the heating furnace is connected to the inlet of the drying section A.

Claims (2)

[Claims] (1) To recover oil and combustible gas by thermally decomposing oil shale, first, a layer of oil shale agglomerates consisting of coarse particles is formed on a horizontal surface, and the layer is continuously moved by water. Preheating the grain agglomerates at a temperature of 100 to 350° C. in a range that does not cause extensive drying of the hydrocarbon compounds contained in the wrinkled grain agglomerates by flowing a preheated drying gas through the bed in one section; Second zone I, drying and then carbonizing the layer
The hydrocarbon compounds contained in the preheated and dried granules are carbonized in the first zone by passing through the IK, and the carbonized product is cooled and air heated. The oil and combustible gas are separated by liquid separation, and the agglomerates with different particle sizes are pulverized and adjusted to the particle size necessary to maintain the fluidized bed state. The powder and granules are transferred to the subsequent combustion process, where a fluidized bed is formed by a flow of oxygen-containing gas, and the heat is recovered while burning the combustible materials that could not be heated in the carbonization T'8, and the remaining The powder and granules are transferred to the final cooling process, where a fluidized bed is formed by the cooling gas fiK, and the sensible heat held by the residual sound powder is transferred to the cooling gas, and the cooled waste solids are removed from the system. A method for recovering oil and gas from oil shale, characterized by recovering heat from the exhaust gas of the cooling process. (2) A moving grid installed in the horizontal direction and configured to be movable continuously in one direction along the flfi, and a wind box separated by two partitions that cross the moving grid, one of which has a preheating , a dry gas inlet on the other side, a dry exhaust gas outlet on the other side, an oil shale supply inlet on the upper part of the moving grid of the partition wall a on the upstream side with respect to the moving direction of the partition walls, and an oil shale supply port on the upper part of the moving grid of the partition wall A on the downstream side. The drying section is divided into 8 drying sections each having nine preheated and dried grain agglomerate outlets, and the section 11b and the section i on the downstream side thereof. Carbonization section B comprising a semi-parabolic outlet and a 115kll granule agglomerate outlet on the moving grid of the partition wall CCt.
A crushing device having a residual granule inlet on one side and a powder outlet on the other, and a body inlet opening at the middle lower part of the fluidized bed formed inside the crushing device. A combustion tower is formed in the middle upper part of the wrinkled fluidized bed, which is equipped with an Fi residue * granule outlet, a part with an oxygen-containing gas inlet, and a combustion gas outlet in the upper part. The high temperature residual powder inlet is placed at the middle lower part of the bed, and the middle upper part of the fluidized bed I! A cooling tower consisting of an integrated IR outlet cooled by Maqin, a cooling gas inlet in the lower part, and a cooling exhaust gas outlet in the upper part, a dry powder inlet on one side, and a carbonization product gas outlet and a carbonization product gas outlet on the other side. I
A heating furnace that heats the IA is installed in parallel, and the movable grating device on
The granule agglomerate outlet and the residual granule inlet of the crushing device, the powder and granule outlet of the crusher, the powder and granule inlet of the combustion tower, the residual powder and granule outlet of the combustion tower and the residual powder and granule inlet of the cooling tower. In addition to cooling the carbonization product outlet of the carbonization section B, the carbonization product gas heated in the heating furnace is passed through the carbonization section B to the carbonization product gas heated in the heating furnace. 1. Also, the combustion exhaust gas of the heating furnace is transferred to the drying zone H.
A device for recovering oil and gas from oil shale, which is characterized by a swell formed at the entrance of a person.