CN109401784B

CN109401784B - Comprehensive utilization method of heavy inferior oil and oil shale

Info

Publication number: CN109401784B
Application number: CN201811526974.8A
Authority: CN
Inventors: 王重平; 陈兆然; 马骏
Original assignee: Shanghai Boshen Engineering Technology Co ltd
Current assignee: Shanghai Boshen Engineering Technology Co ltd
Priority date: 2018-12-13
Filing date: 2018-12-13
Publication date: 2023-10-20
Anticipated expiration: 2038-12-13
Also published as: CN109401784A

Abstract

The invention discloses a comprehensive utilization method and device of heavy inferior oil and oil shale, in particular to a device which is provided with a carbonization reactor (A), a carbonization pre-reactor (C), a cracking reactor (B), a cracking pre-reactor (D), a settler (E), a mixer (F), a gasifier (G), a combustor (H), a heat collector (I), a quencher (J) and a scrubber (K); the connection method is detailed in the specification; a comprehensive utilization method adopting the device is also disclosed. The invention organically combines heavy inferior oil cracking, oil shale carbonization, oil-gas separation and dust removal, dust-containing heavy oil and middle extraction oil recycling and shale semicoke heat exchange/gasification/calcination/heat extraction in a set of device, thereby obtaining clean oil gas with high added value, high heat value synthesis gas and shale ash products.

Description

Comprehensive utilization method of heavy inferior oil and oil shale

Technical Field

The invention belongs to the field of petroleum processing and oil shale processing, and relates to a comprehensive utilization method and device of heavy inferior oil and oil shale.

Background

In the petroleum processing field, heavy inferior oil (such as inferior vacuum residue, high viscosity heavy oil and the like) has great concentration and high impurity content (such as high metal content, high solid content and high sulfur), so that the processing difficulty of the heavy inferior oil is great and the main processing technology of the existing heavy inferior oil is as follows: the delayed coking process has strong raw material adaptability, but has low liquid product yield, low petroleum coke product added value and larger environmental pollution; the hydrogenation process has the advantages of high yield of liquid products, environmental friendliness, complex process, large investment, high processing cost and poor raw material adaptability; the flexible coking process has strong raw material adaptability and higher liquid product yield, but the flexible gas product has low heat value, difficult utilization and high operation difficulty. Therefore, how to develop a heavy inferior oil processing technology with lower cost, higher raw material utilization rate, higher added value of products and more friendly environment on the basis of the prior art is always an urgent need for heavy inferior oil processing.

Oil shale, also known as "oil shale", is a fine sedimentary rock rich in organic matter and having fine layering. Most of organic matters in the oil shale are oil-forming matters insoluble in common organic solvents, commonly called 'kerogen', and the kerogen consists of complex high-molecular organic compounds, so that shale oil can be extracted. Incomplete statistics indicate that global oil shale reserves are huge in resource quantity, estimated to be 10 trillion tons (more than 5000 billion tons of refined shale oil), and are mainly distributed in countries such as the United states, zaire, brazil, italy, morocco, jordan, australia, china and Canadian. How to more effectively extract shale oil from oil shale and realize high-efficiency comprehensive utilization of the oil shale is always a pursued goal in the field of oil shale processing. At present, among various oil shale technologies applied or developed at present, the oil shale fluidization and carbonization technology becomes a main development direction of technology development due to the advantages of high oil yield, high raw material utilization rate and the like, but the existing applied or developed fluidization and carbonization technology has the problems of difficult oil gas online dust removal, low shale ash utilization with high additional value and the like, and development of a new technology for processing the oil shale with higher efficiency and perfection is needed.

Disclosure of Invention

The invention aims to provide a comprehensive utilization method and device of heavy inferior oil and oil shale.

In order to achieve the above purpose, the present invention provides the following technical solutions:

the device is provided with a carbonization reactor A, a carbonization pre-reactor C, a cracking reactor B, a cracking pre-reactor D, a settler E, a mixer F, a gasifier G, a combustor H, a heat collector I, a quencher J and a scrubber K;

the upper part and the lower part of the settler E are provided with a settling section and a stripping section; comprises a first-stage gas-solid separator Y-1, a second-stage gas-solid separator Y-2 and a gas distributor X-1; the primary gas-solid separator Y-1 is arranged at the upper part inside the settler E; the secondary gas-solid separator Y-2 is arranged inside or outside the settler E; the gas distributor X-1 is arranged at the lower part inside the settler E;

the mixer F is provided with a mixing section and a stripping section at the upper part and the lower part; comprises a gas-solid separator Y-3 and a gas distributor X-2; the gas-solid separator Y-3 is arranged inside or outside the mixer F; the gas distributor X-2 is arranged at the lower part inside the mixer F;

the gasifier G is provided with a gasification section and a stripping section at the upper part and the lower part; comprising a gas distributor X-3; the gas distributor X-3 is arranged at the lower part inside the gasifier G;

The burner H is provided with a combustion section and a stripping section at the upper part and the lower part; comprising a gas distributor X-4; the gas distributor X-4 is arranged at the lower part inside the combustor H;

wherein, the outlet of the carbonization reactor is connected with a first-stage gas-solid separator in the settler, and the inlet is connected with the carbonization pre-reactor; the outlet of the cracking reactor is connected with the settler, and the inlet of the cracking reactor is connected with the cracking pre-reactor; the upper outlet of the settler is connected with a quencher, and the lower outlet of the settler is respectively connected with a carbonization pre-reactor, a cracking pre-reactor and a mixer; the upper part of the mixer is provided with an outlet, and the lower outlet is respectively connected with a carbonization pre-reactor, a cracking pre-reactor and a gasifier; the upper outlet of the gasifier is connected with a gas distributor at the lower part of the mixer, and the lower outlet is connected with a burner; the lower outlet of the burner is connected with the inlet of the heat collector, and the upper outlet of the burner is connected with the inlet of the gasifier; the inlet of the quenching device is connected with a secondary gas-solid separator in the settler, and the outlet of the quenching device is connected with the bottom inlet of the scrubber; the upper part of the scrubber is respectively provided with an outlet connected with the quenching device and the cracking pre-reactor.

Preferably, the device is also provided with a liquid-solid separator L and a heavy oil heat exchanger M; wherein, the outlet of the bottom of the scrubber is connected with the inlet of the liquid-solid separator; the outlet of the liquid-solid separator is respectively connected with the inlet of the carbonization pre-reactor and the heavy oil heat exchanger; the outlet of the heavy oil heat exchanger is connected with the inlet of the middle part of the scrubber.

Preferably, the heavy oil heat exchanger is further provided with a product outlet.

Preferably, the scrubber is also provided with a product outlet.

Preferably, the scrubber is also provided with a raw material inlet.

Preferably, the device is further provided with an oil extraction heat exchanger N; wherein, the inlet and outlet of the oil extraction heat exchanger are respectively connected with the middle part and the upper part of the scrubber.

Preferably, the extracted oil heat exchanger is further provided with a product outlet.

Preferably, the lower outlet of the settler, the carbonization pre-reactor and the cracking pre-reactor are respectively provided with a connecting pipe, and the connecting pipe is provided with a regulating valve.

Preferably, the lower outlet of the settler and the mixer are provided with a connecting pipe, and the connecting pipe is provided with a regulating valve.

Preferably, the outlet at the lower part of the mixer, the carbonization pre-reactor, the cracking pre-reactor and the gasifier are respectively provided with a communicating pipe, and the communicating pipes are respectively provided with regulating valves.

Preferably, the lower outlet of the gasifier and the burner are provided with communicating pipes, and regulating valves are respectively arranged on the communicating pipes.

Preferably, the retorting reactor is provided with an oil shale feed inlet and optionally an external feedstock inlet.

Preferably, the cracking reactor is provided with a heavy inferior oil feed inlet and optionally an external feedstock inlet.

Preferably, the gas distributor is provided with gas inlets.

Preferably, the gas inlet is provided on the connection pipe of the mixer and the gasifier.

The method comprises the following steps of providing the comprehensive utilization device:

(I) Heating the oil shale raw material and the material from the carbonization pre-reactor in the carbonization reactor to carry out carbonization reaction, so as to obtain carbonization reaction material; enabling the carbonization reaction material flowing out of the carbonization reactor to enter a first-stage gas-solid separator in a settler for first separation to obtain carbonization oil gas and carbonization material;

heating a heavy inferior oil raw material and a material from a cracking pre-reactor in a cracking reactor to carry out a cracking reaction to obtain a cracking reaction material; the cracking reaction material flowing out of the cracking reactor enters a settler and is subjected to sedimentation separation in the settler to obtain cracked oil gas and cracked material;

the first separated dry distillation oil gas and the settled and separated cracking oil gas enter a secondary gas-solid separator for secondary separation; the mixed oil gas separated for the second time enters a scrubber through a quencher; returning the solid materials separated for the second time to the settler;

after the first separated dry distillation material, the settled and separated cracking material and the second separated solid material are subjected to degassing in a gas stripping section of the settler, part of the materials are heated in a mixer, part of the materials are subjected to pre-cooling in a dry distillation pre-reactor, and part of the materials are subjected to pre-cooling in a cracking pre-reactor;

(II) after the materials from the settler and the gas from the gasifier are heated in the mixer, the products are separated by a gas-solid separator; the separated gas is sent out as a product; the separated solid material: heating a part of materials in a carbonization pre-reactor, heating a part of materials in a cracking pre-reactor, and carrying out gasification reaction in a gasifier;

(III) obtaining a gas material and a solid material after the gasification reaction is finished; returning the gas material to the mixer; the solid materials enter a burner for further combustion; the solid product after combustion is sent out as shale ash product after heat is recovered by a heat collector; the burnt gas product enters the gasifier, enters the mixer for heat exchange and is sent out as a product after gas-solid separation.

Preferably, the method further comprises the steps of: after the mixed oil gas from the settler passes through the quencher and enters the scrubber,

the solid-containing heavy oil separated from the bottom of the scrubber is sent to a liquid-solid separator for liquid-solid separation; the separated low-solid-content heavy oil is returned to the scrubber as washing liquid or sent out as a product after heat exchange by a heavy oil heat exchanger; the separated high-solid-content heavy oil enters a carbonization pre-reactor to carry out secondary carbonization reaction;

One part of the extracted oil flowing out from the middle part of the scrubber is sent to a cracking pre-reactor for secondary cracking reaction, and the other part is returned to the quencher as quenching oil;

and the cleaned oil gas after washing is taken as a product to be sent out from the top of the washer.

Preferably, the method further comprises the steps of: part of the extracted oil flowing out of the middle part of the scrubber is heated by the extracted oil heat exchanger and then returned to the scrubber to be used as a scrubbing liquid or sent out as a product.

Preferably, the operating conditions of the retorting reactor are: the pressure is 0.1-0.8 MPa, and the temperature is 450-600 ℃.

Preferably, the operating conditions of the dry distillation prereactor are: the pressure is 0.1-0.8 MPa, and the temperature is 480-650 ℃.

Preferably, the cracking reactor is operated under the following conditions: the pressure is 0.1-0.8 MPa, and the temperature is 450-580 ℃.

Preferably, the cracking prereactor operating conditions are: the pressure is 0.1-0.8 MPa, and the temperature is 480-600 ℃.

Preferably, the operating conditions of the settler are: the pressure is 0.1-0.8 MPa, and the temperature is 450-600 ℃.

Preferably, the operating conditions of the mixer are: the pressure is 0.1-0.8 MPa, and the temperature is 560-800 ℃.

Preferably, the operating conditions of the gasifier are: the pressure is 0.1-0.8 MPa, and the temperature is 800-1200 ℃.

Preferably, the operating conditions of the burner are: the pressure is 0.1-0.8 MPa, and the temperature is 850-1400 ℃.

Preferably, the operating conditions of the quench cooler are: the pressure is 0.1-0.8 MPa, and the temperature is 350-480 ℃.

Preferably, the operating conditions of the scrubber are: the pressure is 0.1-0.8 MPa, and the temperature is 80-400 ℃.

Preferably, the linear velocity of the gas in the carbonization reactor is 0.2-8.0 m/s.

Preferably, the linear velocity of the gas in the carbonization pre-reactor is 0.2-8.0 m/s.

Preferably, the cracking reactor gas line velocity is from 0.2 to 8.0 m/s.

Preferably, the gas linear velocity of the cracking prereactor is 0.2-8.0 m/s.

Preferably, the upper gas line speed of the settler is 0.1-3.0 m/s.

Preferably, the upper gas line speed of the mixer is 0.1-3.0 m/s.

Preferably, the upper gas line speed of the gasifier is 0.01-5.0 m/s.

Preferably, the upper gas line speed of the burner is 0.01-5.0 m/s.

Preferably, the heavy inferior oil raw material is a flowing substance (such as liquid or solid-containing liquid) containing hydrocarbon; wherein the flowable substance is selected from one or more of the following group: heavy oil, residual oil, tar, slurry oil, swill-cooked dirty oil, waste oil, dirty oil and shale oil; the solids content of the flowable substance is less than 15% by weight.

Preferably, the mobile material element range preferably: hydrogen content 7-20 wt%, and carbon content 75-92 wt%.

Preferably, the particle size of the oil shale raw material is not more than 8 mm.

Preferably, the particle size ranges from 0.03 to 3 mm.

Preferably, the oil shale material may incorporate a hydrocarbon-containing solid material; wherein the hydrocarbon-containing solid material is selected from one or more of the following group: lignite, bituminous coal with a caking index gr.i. <50, long flame coal, anthracite, sludge, and oil sludge; the grain diameter of the solid matters containing hydrocarbon is less than or equal to 8 mm; the proportion of the hydrocarbon-containing solid matter is less than or equal to 50% by weight.

Preferably, the ratio of the heavy inferior oil raw material to the oil shale raw material is as follows: 5%:95% -95%: 5% by weight.

The technical scheme of the invention has the following advantages:

(1) According to the invention, the shale semicoke produced after the oil shale is fluidized and distilled is used as a heat supply carrier, the heavy inferior oil is fluidized and cracked in the cracking reactor and the oil shale is fluidized and distilled in the carbonization reactor, and as the cracking reactor and the carbonization reactor can be separately temperature-controlled and the forced back mixing structure is arranged in the cracking reactor and the carbonization reactor to achieve the full back mixing effect, the rapid mass transfer and heat transfer are realized, and the uniformity of the temperature field in the reactor is ensured, therefore, the invention can accurately control the reaction temperature by adjusting the high-temperature shale semicoke supply amount, and the fluidized cracking reaction of the heavy inferior oil and the fluidized and distilled reaction of the oil shale are carried out at proper temperature, thereby realizing the maximization of the liquid oil yield and the shale oil yield of the oil shale carbonization.

(2) According to the invention, the shale semicoke produced after the oil shale is fluidized and dry distilled is used as a fluidization carrier, the heavy inferior oil fluid cracking reaction raw coke is carried on the shale semicoke, the shale semicoke is sent to a subsequent gasifier, and the heavy inferior oil cracking raw coke and the oil shale dry distillation raw coke are fluidized and gasified together in the gasifier, so that the low-value coke is converted into a high-value synthesis gas product. Because shale semicoke mainly comprises inorganic matters, the particle structure is stable and the fluidization performance is good, the shale semicoke is used as a fluidization carrier to realize the stable operation of heavy inferior oil fluidization cracking, oil shale fluidization carbonization and shale semicoke fluidization gasification, and the problems of unstable fluidization operation and the like caused by unstable self-produced coke particle size and poor fluidization performance of the heavy inferior oil individual fluidization cracking can be avoided.

(3) The impurities such as metal contained in the heavy inferior oil fluid cracking raw coke carried on the shale semicoke are discharged along with the shale ash, and the discharge amount of the shale ash is large, so that the impurities such as metal deposited on the shale semicoke in a reaction system can be ensured to be in a lower concentration range, the influence of the impurities such as metal on the cracking of the heavy inferior oil is reduced to the greatest extent, unnecessary secondary cracking and other side reactions are reduced, and the yield of liquid oil is improved.

(4) According to the invention, the heavy inferior oil is gasified by the fluid cracking raw coke and the oil shale carbonization raw coke, and meanwhile, the original carbon in the oil shale is gasified, so that the yield of gasified synthetic gas is improved, and the problem of insufficient heat supplied to the cracking reaction and carbonization reaction due to small gasification synthetic gas quantity caused by small reaction raw coke quantity is avoided.

(5) The invention separates and removes dust from the cracked oil gas and the dry distillation oil gas, and then sends out the oil gas, which can realize the following beneficial effects: a. the quality of liquid oil in the dry distilled oil gas is relatively good, so that the quality of liquid oil of a heavy inferior oil cracking product can be improved after mixing; b. because the dry gas content in the dry distillation oil gas is higher, the liquid oil product is relatively lower, the subsequent separation of the dry gas and the liquid oil is relatively difficult, the dry gas content in the cracked oil gas is lower, the liquid oil content is relatively higher, the subsequent separation of the dry gas and the liquid oil is relatively easy, and the subsequent separation is carried out after the dry distillation oil gas and the cracked oil gas are mixed, so that the component complementation can be realized, and the subsequent separation difficulty is reduced.

(6) The invention combines the heavy inferior oil and the oil shale, and can solve the problems that the oil shale industry popularization is difficult and the like caused by the influence on project economic benefit due to the fact that the oil yield is low and the large-scale processing is difficult to form in the pure oil shale processing.

(7) According to the invention, shale semicoke is used as a carrier, and the main component of the shale semicoke is inorganic, so that the concentration of carried coke and carbon is low, and the problems that the gasification operation is influenced by over-temperature caused by high concentration of coke and carbon can not occur when oxygen enrichment or pure oxygen gasification is adopted in the gasifier.

(8) According to the invention, the carbonization pre-reactor is arranged in front of the carbonization reactor, on one hand, the separated solid-containing heavy oil is subjected to on-line recycling and cracking, so that not only is no or less low-value solid-containing heavy oil avoided, but also the yield of high-value light oil can be increased, and the added value of the product is improved; on the other hand, the high-temperature shale semicoke is subjected to primary pre-cooling before entering the carbonization reactor through the carbonization pre-reactor, so that the problem that the partial high temperature is caused by the fact that the shale semicoke with excessive high temperature directly enters the carbonization reactor, so that the carbonization oil gas is subjected to secondary cracking, and the oil yield is reduced is avoided.

(9) According to the invention, the cracking pre-reactor arranged in front of the cracking reactor can carry out on-line recycling cracking on the extracted medium oil, so that the yield of high-value light oil is increased, and the added value of the product is improved; on the other hand, the high-temperature shale semicoke is subjected to primary pre-cooling before entering the cracking reactor through the cracking pre-reactor, so that the problem that the cracking oil gas is subjected to secondary cracking to a large extent to reduce the oil yield due to the fact that the shale semicoke with the excessive temperature directly enters the cracking reactor to cause local high temperature is avoided.

(10) The dry distillation reaction product passes through the first-stage gas-solid separator to realize the rapid separation of oil gas and shale semicoke, so that the phenomenon that the oil yield is reduced due to the fact that the secondary cracking reaction is more after the oil generated by the dry distillation reaction contacts the high-temperature shale semicoke for a long time is avoided; the dry distillation oil gas passing through the first-stage gas-solid separator and the cracked oil gas from the cracking reactor pass through the settler and the second-stage gas-solid separator, so that most of fine powder solids in the mixed oil gas are separated, and the burden of subsequent washing and dust removal of the mixed oil gas is greatly reduced. In addition, the gas stripping section arranged at the lower part of the settler is used for stripping gas entrained in the solid through injected gas, so that the entrained oil gas is prevented from being carried into a subsequent mixer, and the oil gas yield is reduced.

(11) The mixer provided by the invention utilizes the characteristic that the fluidized bed can rapidly achieve sufficient heat transfer, the high-temperature solid-containing synthetic gas generated by the gasifier heats shale semicoke in the mixer, a part of the heated shale semicoke is circulated to the reactor for heat supply, and the other part of the heated shale semicoke is calcined to different degrees at high temperature according to the subsequent requirements in the combustor to obtain high-value shale ash products (which can be used as high-quality raw materials of cement, building materials and the like), so that the heat of the high-temperature solid-containing synthetic gas is fully utilized, the cascade utilization of different grade heat is realized, the energy utilization efficiency is improved, and the heat supply cost and energy consumption are reduced.

(12) According to the invention, the high-temperature shale ash after calcination is subjected to a closed multi-stage heat exchange mode, so that the energy cascade recovery is realized, a low-temperature shale ash product can be obtained, and the problem of dry cooling of the shale ash is well solved.

(13) According to the invention, the high-temperature multistage gas-solid separation and low Wen Duoduan washing are combined for the solid-containing oil gas, so that clean oil gas is obtained through online dust removal, the added value of the product is improved, and the problem that the oil gas is difficult to online dust removal in the existing fluidized carbonization and cracking method is well solved.

(14) The cracking reactor and the carbonization reactor realize the fluid cracking of the heavy inferior oil and the fluid carbonization of the oil shale, simultaneously re-crack the fluid substances containing hydrocarbon (liquid or solid-containing liquid such as tar, slurry oil, swill-cooked dirty oil, waste oil and the like) and also can be doped with the solid containing hydrocarbon such as powdered coal, oil sand, oil sludge, sludge and the like, thereby realizing the mixed processing of various liquid and solid substances.

(15) According to the invention, the heavy inferior oil and the oil shale are processed in a set of device in a combined way, and the heavy inferior oil is subjected to fluid cracking, fluid dry distillation, oil-gas separation and dust removal, dust-containing heavy oil and middle extracted oil recycling, shale semicoke heat exchange/gasification/calcination/heat extraction are organically combined, so that clean oil gas with high added value, high heat value synthesis gas and shale ash products are obtained.

Drawings

Fig. 1 is a schematic diagram of a comprehensive utilization device of heavy inferior oil and oil shale.

Detailed Description

The invention is further elucidated below in connection with the accompanying drawings. The detailed description and examples are not intended to limit the scope of the invention as claimed.

As shown in fig. 1, the invention relates to a comprehensive utilization device of heavy inferior oil and oil shale:

the device is provided with a carbonization reactor A, a carbonization pre-reactor C, a cracking reactor B, a cracking pre-reactor D, a settler E, a mixer F, a gasifier G, a combustor H, a heat collector I, a quencher J, a scrubber K, a liquid-solid separator L, a heavy oil heat exchanger M and an extracted oil heat exchanger N.

The outlet of the carbonization reactor A is connected with a first-stage gas-solid separator Y-1 in the interior of the settler E, and the inlet is connected with the carbonization pre-reactor C. The outlet of the cracking reactor B is connected with the settler E, and the inlet is connected with the cracking pre-reactor D. The top of the settler E is provided with a secondary gas-solid separator Y-2 which can be arranged inside or outside the settler; the lower part of the settler E is provided with a gas distributor X-1. The lower outlet of the settler, the carbonization pre-reactor C and the cracking pre-reactor D are respectively provided with a connecting pipe, and the connecting pipes are provided with regulating valves a and b. The lower outlet of the settler and the mixer F are provided with a connecting pipe, and the connecting pipe is provided with a regulating valve c. The upper part of the mixer is provided with a gas-solid separator Y-3 which can be arranged inside or outside the mixer. The lower part of the mixer is provided with a gas distributor X-2, the outlet of the lower part of the mixer is provided with communicating pipes which are communicated with the carbonization pre-reactor C, the cracking pre-reactor D and the gasifier G, and the communicating pipes are respectively provided with regulating valves D, e and f. The upper inlet of the gasifier G is connected with a gas distributor X-2 at the lower part of the mixer F, and the lower outlet of the gasifier G is connected with a combustor H. The lower outlet of the burner H is connected with the inlet of the heat collector I, and the upper outlet of the burner H is connected with the gasifier G. The second-stage gas-solid separator Y-2 of the settler E is connected with the inlet of the quencher J, the outlet of the quencher J is connected with the inlet at the bottom of the scrubber K, and the outlet at the bottom of the scrubber K is provided with a communicating pipe with the liquid-solid separator L. The outlet of the liquid-solid separator L is respectively connected with the inlets of the carbonization pre-reactor C and the heavy oil heat exchanger M, the outlet of the heavy oil heat exchanger M is connected with the washer K, the inlet and the outlet of the middle oil extraction heat exchanger N are respectively connected with the middle part and the upper part of the washer K, and the upper part of the washer K is provided with an outlet which is connected with the quencher J and the cracking pre-reactor D.

The carbonization reactor A adopts a fluidization type, a forced back mixing structure with a flow dividing and baffling function is arranged in the carbonization reactor A, and powdery oil shale feeding 1, optional external raw materials 3 and high-temperature materials 5 from a carbonization pre-reactor C can be quickly subjected to sufficient back mixing and mass and heat transfer to obtain a product 7, so that the reaction temperature in the carbonization reactor is uniform, the reaction temperature in the carbonization reactor can be accurately controlled by adjusting the supply amount of high-temperature heat supply shale semicoke, and the carbonization of the oil shale at a proper temperature is realized, thereby obtaining the maximum oil yield. The particle size of the powdery oil shale feed 1 is not more than 8 mm, and the preferred particle size range is: 0.03-3 mm; the external raw material 3 is a solid substance containing hydrocarbon, preferably lignite, bituminous coal with a caking index gr.i. <50, long flame coal, anthracite, oil sludge, etc. The solid matter has a particle size of not more than 8 mm, preferably in the particle size range: 0.03-3 mm. The blending proportion of the extraneous raw material 3 is not more than 80% by weight of the oil shale feed 1. The operating conditions of the retorting reactor A were: the pressure is 0.1-0.8 MPa, the temperature is 450-600 ℃, and the gas linear velocity is 0.2-8.0 m/s.

The carbonization pre-reactor C mixes the carbonized shale semicoke 13 stripped by the precipitator E, the heating material 6 from the mixer F and the high-solid-content heavy oil 44 from the liquid-solid separator L to obtain a product 5. The inside of the carbonization pre-reactor C is provided with a back mixing structure with the flow dividing and baffling functions, so that the full back mixing contact of carbonization shale semicoke, heating shale semicoke and high-solid-content heavy oil is ensured, the carbonization pre-reactor on one hand carries out on-line back refining and cracking on the separated solid-content heavy oil, thereby avoiding the non-production or less-production of low-value solid-content heavy oil, increasing the high-value light oil yield and greatly improving the added value of products; on the other hand, the high-temperature shale semicoke is subjected to primary pre-cooling before entering the carbonization reactor through the carbonization pre-reactor, so that the problem that the oil component is subjected to secondary pyrolysis to a large extent to reduce the oil yield due to the fact that the excessive high-temperature heat supply shale semicoke directly enters the carbonization reactor is avoided. The operating conditions of the dry distillation prereactor C were: the pressure is 0.1-0.8 MPa, the temperature is 480-650 ℃, and the gas linear velocity is 0.2-8.0 m/s.

The cracking reactor B adopts a fluidization type, a forced back mixing structure with a flow dividing and baffling function is arranged in the cracking reactor B, and the heavy inferior oil feed 2, optional external raw materials 4 and high-temperature materials 15 from the cracking pre-reactor D can be quickly subjected to sufficient back mixing and mass and heat transfer to obtain a product 16, so that the reaction temperature in the cracking reactor is uniform, the reaction temperature in the cracking reactor can be accurately controlled by adjusting the supply amount of the shale semicoke with high-temperature heat supply, and the cracking of the heavy inferior oil at a proper temperature is realized, thereby obtaining the maximized light oil yield. The heavy inferior oil feed 2 is a hydrocarbon-containing mobile material (liquid or solid-containing liquid). The flow material element range is preferably: hydrogen content 7-20 wt%, and carbon content 75-92 wt%. The type of flowable substance is preferably: heavy oil, residual oil, tar, slurry oil, swill-cooked dirty oil, shale oil and the like. The solids content of the above-mentioned preferred flowable substances is preferably less than 15% by weight. The external raw material 4 is a solid substance containing hydrocarbon, preferably lignite, bituminous coal with a caking index gr.i. <50, long flame coal, anthracite, sludge, etc. The solid matter has a particle size of not more than 8 mm, preferably in the particle size range: 0.03-3 mm. The blending ratio of the extraneous raw material 4 is not more than 50% by weight of the heavy inferior oil feed 2. The operating conditions of the cracking reactor B were: the pressure is 0.1-0.8 MPa, the temperature is 450-580 ℃, and the gas linear velocity is 0.2-8.0 m/s.

The cracking pre-reactor D mixes the dry distilled shale semicoke 14 stripped by the precipitator E, the heating material 22 from the mixer F and the middle extracted oil 48 from the scrubber K by introducing the lifting gas 23 to obtain a product 15. The inside of the cracking pre-reactor D is provided with a back mixing structure with the flow dividing and baffling functions, so that the full back mixing contact of the dry distillation shale semicoke, the heat supply shale semicoke and the middle extracted oil is ensured, the separated middle extracted oil is subjected to on-line back refining cracking by the cracking pre-reactor on one hand, the high-value light oil yield is increased, and the added value of the product is greatly improved; on the other hand, the high-temperature shale semicoke is subjected to primary pre-cooling before entering the cracking reactor through the cracking pre-reactor, so that the problem that the oil component is subjected to secondary cracking to a large extent to reduce the oil yield due to the fact that the excessive high-temperature heat supply shale semicoke directly enters the cracking reactor is avoided. The operating conditions of the cracking prereactor D were: the pressure is 0.1-0.8 MPa, the temperature is 480-600 ℃, and the gas linear velocity is 0.2-8.0 m/s.

The primary gas-solid separator Y-1 is arranged in the settler E, so that the dry distillation reaction material 7 from the A can realize the rapid separation of oil gas and solid through the primary gas-solid separator, and the secondary cracking of the oil product after the long contact time of the oil gas generated by dry distillation and the high-temperature solid can be reduced as much as possible, thereby reducing the oil yield. The primary gas-solid separator is preferably an inverted L-shaped separator, a single-stage cyclone separator and other structural types. The solid-containing oil gas 8 separated by the first-stage gas-solid separator is mixed with the cracked solid-containing oil gas which is obtained by the reaction product 16 from the cracking reactor B and enters a settler for sedimentation to form 10, the 10 enters a second-stage gas-solid separator Y-2 for secondary dust removal of the mixed oil gas, the oil gas 11 with the content of the solid fine powder separated by the second-stage gas-solid separator being greatly reduced enters a quencher J, and the solid fine powder 12 separated by the second-stage gas-solid separator returns to the settler. The secondary gas-solid separator Y-2 is preferably a two-stage cyclone separator, the inlet linear velocity of which is 10-40 m/s, and can be arranged inside or outside the settler E. The solid 9 separated from the dry distillation reaction material 7 by the first-stage gas-solid separator Y-1 and the solid after the cracking reaction product 16 enters the settler to be settled enter a gas stripping section at the lower part of the settler, and gas stripping gas 24 is injected into the gas stripping section through a gas distributor X-1 to remove oil gas entrained in the solid to obtain 17, so that the entrained oil gas is prevented from being carried to a mixer to reduce the oil yield. The lower part of the settler is provided with a herringbone baffle or an annular baffle or other structures for improving the countercurrent contact of gas and solid, thereby improving the stripping effect. The stripping gas 24 may be one or more of the following gases: steam, dry gas, hydrogen, methane gas, ethane gas, light hydrocarbon gas, nitrogen, carbon dioxide, flue gas, etc., wherein steam or self-produced dry gas is preferable as stripping gas. The operating conditions of the settler E were: the pressure is 0.1-0.8 MPa, the temperature is 450-600 ℃, and the upper gas linear velocity is 0.1-3.0 m/s.

The upper part of the mixer F is a solid sedimentation section, and the lower part is a heat exchange section. Solids 17 from the settler E are lifted 19 via a control valve c into the mixer F via a lift gas 18 and mixed with the high temperature solids-laden syngas 31 from the gasifier G for heat exchange. The heat exchange section preferably adopts a turbulent fluidized bed type, and the gas distributed by the gas distributor X-2 improves the flow field distribution in the heat exchange section so as to achieve a sufficient heat exchange effect. The gas after heat exchange enters a gas-solid separator Y-3 after passing through an upper solid sedimentation section to form 27, and the synthesis gas 28 after most of solid fine powder is separated out is sent out to be used as a product; the solid fines 29 are returned to the mixer F. The solid material 20 from the mixer is lifted to the carbonization pre-reactor C through the lifting gas 21 via the regulating valve D, the solid material 22 from the mixer is transferred to the cracking pre-reactor D through the regulating valve e, and the solid material 30 from the mixer is transferred to the gasifier G through the regulating valve f. The gas-solid separator Y-3 is preferably a two-stage cyclone separator, the inlet linear velocity of which is 10-40 m/s, and can be arranged inside or outside the mixer F. The high-temperature heat of the high-temperature solid-containing synthetic gas from the gasifier G is utilized to the maximum extent through the heater F, and besides the heat supply of the high-temperature solid-containing synthetic gas, the heat release and the heat supply can also be realized through the reaction of the oxygen-containing gas 36 and the organic components in the shale semicoke, or the heat supply of the external high-temperature gas 40 can be directly supplemented. The oxygen-containing gas 36 is preferably: air, oxygen-enriched gas, oxygen, air-steam mixture, oxygen-steam mixture. The external high temperature gas 40 preferably: high temperature synthesis gas and high temperature raw gas. The operating conditions of mixer F were: the pressure is 0.1-0.8 MPa, the temperature is 560-800 ℃, and the gas linear velocity is 0.1-3.0 m/s.

Shale semicoke 30 from mixer F is controlled by regulating valve F to enter gasifier G for gasification reaction with oxygen-containing gas 37 and optional external fuel 38 passing through gas distributor X-3 to obtain shale semicoke 32 and solids-containing synthesis gas 31. The oxygen-containing gas 37 is preferably: oxygen and steam mixed gas, oxygen-rich and steam mixed gas and air and steam mixed gas; the extraneous fuel 38 is preferably: dry distillation gas, dry gas, natural gas and raw gas. The operating conditions of the gasifier G were: the pressure is 0.1-1.0 MPa, the temperature is 800-1200 ℃, and the gas linear velocity is 0.01-5.0 m/s.

Shale semicoke 32 from gasifier G is controlled by regulating valve G to enter burner H to react with oxygen-containing gas 39 passing through gas distributor X-4 for releasing heat, and calcined shale ash 34 and solid-containing gas 33 are obtained. The oxygen-containing gas 39 is preferably: air, oxygen-enriched gas, oxygen, air-steam mixture, oxygen-steam mixture. The shale semicoke in the combustor can be calcined at high temperature to different degrees according to the subsequent requirements, so that a high-value shale ash product (which can be used as raw materials of high-quality cement, building materials and the like) is obtained. The operating conditions of the burner H are: the pressure is 0.1-1.0 MPa, the temperature is 850-1400 ℃, and the gas linear velocity is 0.01-5.0 m/s.

The calcined shale ash 34 discharged from the burner H enters the heat collector I for heat recovery as shale ash product 35. The heat collector can adopt the following modes according to the product temperature requirement: primary heat extraction, secondary heat extraction, primary heat extraction, secondary heat extraction and tertiary heat extraction. The heat collector can adopt a direct cooling or indirect cooling mode, and the cooling medium can be selected from: the temperature of the shale ash product is controlled to be 30-700 ℃ by a heat collector through water, steam, flue gas, inert gas (nitrogen and carbon dioxide), pyrolysis gas, raw gas, synthesis gas and the like.

The lifting gas 21 and 23 are preferably: pyrolysis gas, raw gas, dry gas, natural gas, the lift gas 18 is preferably: steam, synthesis gas, air-steam mixture, oxygen-steam mixture.

The high-temperature oil gas 11 from the second-stage gas-solid separator Y-2 after most of solids are separated is cooled by the quenching oil 47 from the scrubber K to quench the high-temperature oil gas 11 below a certain temperature, so that cracking and coking of oil products in the oil gas can be avoided to the greatest extent, and equipment and pipelines can be prevented from being blocked. The operating conditions of the quench cooler J were: the pressure is 0.1-0.8 MPa, and the temperature is 350-480 ℃.

The scrubber K is divided into an upper section and a lower section. The mixture 41 of quenching oil and oil gas enters the lower section of the scrubber, and the oil gas is in countercurrent contact with the scrubbing oil 45 from M in the ascending process of the lower section of the scrubber to carry out gas-liquid separation and further remove dust. The lower section of the scrubber is provided with a scrubbing liquid distribution structure, a herringbone baffle or an annular baffle or other structures for improving countercurrent contact of gas and liquid, so that the gas-liquid contact effect is improved. The solid-containing heavy oil 42 separated from the lower section of the scrubber K is subjected to liquid-solid separation in the liquid-solid separator L, the separated low-solid-containing heavy oil 43 enters the heat exchanger M to exchange heat and then returns to the scrubber K as washing oil to be subjected to countercurrent gas-liquid separation and dust removal with the mixture entering the bottom of the scrubber K, the low-solid-containing heavy oil 46 after heat exchange can also be sent out as a product, and the high-solid-containing heavy oil 44 separated from the liquid-solid separator L is returned to the carbonization pre-reactor C to be recycled, so that the low-value solid-containing heavy oil with no or less yield is avoided, the high-value light oil yield is increased, and the added value of the product is greatly improved. The liquid-solid separator L is preferably a sedimentation separation and cyclone separation system. The middle part of the scrubber is pumped out of the oil 48 to the cracking pre-reactor D for recycling, so that the high-value light oil yield can be increased. The oil 49 pumped from the middle part of the scrubber returns to the upper part of the scrubber after passing through the heat exchanger N, and is subjected to secondary countercurrent gas-liquid separation and dust removal with the oil gas entering the upper part of the scrubber F, and a scrubbing liquid distribution structure, a separation tray or a separation filler or other structures for improving gas-liquid countercurrent contact are arranged at the upper section of the scrubber, so that the gas-liquid contact effect is improved. The clean oil gas 52 after the heavy oil is separated by two-stage separation and washing is sent out from the top of the washer, and the clean oil product and clean dry gas can be separated subsequently: the clean oil product has low heavy oil content and high light oil content, and is favorable for subsequent processing into high added value products such as liquefied gas, gasoline, diesel oil or aromatic hydrocarbon; the clean dry gas has high hydrogen and methane content, and can extract hydrogen and methane products with high added value. The scrubber K can be supplemented with the external raw material 53 to the lower section of the scrubber for countercurrent separation and dust removal with oil gas, and the external raw material 53 is preferably the following liquid or solid-containing liquid: heavy oil, residual oil, tar, slurry oil, swill-cooked dirty oil, shale oil and the like. The operating conditions of the scrubber K were: the pressure is 0.1-0.8 MPa, and the temperature is 80-400 ℃. The operating conditions of the liquid-solid separator L were: the pressure is 0.1-2.0 MPa, and the temperature is 80-400 ℃. The operating conditions of the heat exchanger M are: the pressure is 0.1-1.5 MPa, and the temperature is 120-340 ℃. The operating conditions of the heat exchanger N are: the pressure is 0.1-1.5 MPa, and the temperature is 105-250 ℃.

The device is preferably characterized in that: the length of the carbonization reactor A is 1-15 meters; the length of the carbonization pre-reactor C is 1-10 meters; the length of the cracking reactor B is 1-15 m; the length of the carbonization pre-reactor D is 1-10 meters; the length of the settler E is 3-40 m; the length of the heater F is 3-40 meters; the length of the gasifier G is 3-40 meters; the length of the burner H is 3-30 meters; the length of the washer K is 5-40 m.

Examples

The device for processing the heavy inferior oil and the oil shale is adopted to process the following raw materials. The raw materials are mixture of heavy inferior oil and oil shale; the mass composition of the heavy inferior oil and the oil shale is as follows: 50 percent to 50 percent.

The main properties of the heavy inferior oil adopted by the device are shown in table 1.

The main properties of the oil shale adopted by the device are shown in Table 2.

TABLE 1 major Properties of heavy inferior oil

Project	Unit (B)	Numerical value	Remarks
				Density of	d ₄ ²⁰	1.02
Carbon residue value	Weight percent	20.0
				Hydrogen content	Weight percent	8.5
Sulfur content	Weight percent	3.0

TABLE 2 oil shale primary Properties

Project	Unit (B)	Numerical value	Remarks
				Moisture content	Weight percent	5.0
Ash + carbon containing	Weight percent	78.0
				Volatile matters	Weight percent	16.5
Sulfur content	Weight percent	0.5

The particle size range of the raw materials is as follows: particle diameter is less than 3mm, and the range of 0.1-1 mm is more than 50%;

(1) The operation method comprises the following steps:

the apparatus is as described in figure 1.

The carbonization reactor A adopts a fluidization type, a forced back mixing structure with a flow dividing and baffling function is arranged in the carbonization reactor A, and the powdery oil shale feed 1 and the high-temperature material 5 from the carbonization pre-reactor C are fully back mixed and subjected to mass transfer and heat transfer to obtain a product 7.

The carbonization pre-reactor C mixes the carbonized shale semicoke 13 stripped by the precipitator E, the heating material 6 from the mixer F and the high-solid-content heavy oil 44 from the liquid-solid separator L to obtain a product 5. The inside of the carbonization pre-reactor C is provided with a back mixing structure with the functions of flow dividing and baffling.

The cracking reactor B adopts a fluidization type, a forced back mixing structure with a flow dividing and baffling function is arranged in the cracking reactor B, and the heavy inferior oil feed 2 and the high-temperature material 15 from the cracking pre-reactor D are quickly subjected to sufficient back mixing and mass and heat transfer to obtain a product 16.

The cracking pre-reactor D mixes the dry distilled shale semicoke 14 stripped by the precipitator E, the heating material 22 from the mixer F and the middle extracted oil 48 from the scrubber K by introducing the lifting gas 23 (dry gas) to obtain a product 15. The inside of the cracking pre-reactor D is provided with a back mixing structure with a flow dividing and baffling function.

The inside of the settler E is provided with a first-stage gas-solid separator Y-1, so that the dry distillation reaction material 7 from the A can realize the rapid separation of oil gas and solid through the first-stage gas-solid separator. The first-stage gas-solid separator is an inverted L-shaped separator. The solid-containing oil gas 8 separated by the first-stage gas-solid separator is mixed with the cracked solid-containing oil gas which is obtained by the reaction product 16 from the cracking reactor B and enters a settler for sedimentation to form 10, the 10 enters a second-stage gas-solid separator Y-2 for secondary dust removal of the mixed oil gas, the oil gas 11 with the content of the solid fine powder separated by the second-stage gas-solid separator being greatly reduced enters a quencher J, and the solid fine powder 12 separated by the second-stage gas-solid separator returns to the settler. The second-stage gas-solid separator Y-2 adopts a two-stage cyclone separator and is arranged at the top of the settler E. The solid 9 separated from the dry distillation reaction material 7 by the first-stage gas-solid separator Y-1 and the solid after the cracking reaction product 16 enters the settler to be settled enter a gas stripping section at the lower part of the settler, and gas stripping gas 24 (steam) is injected into the gas stripping section through a gas distributor X-1 to remove oil gas entrained in the solid to obtain 17. The lower part of the settler is provided with a herringbone baffle plate to improve the structure of gas-solid countercurrent contact.

Solids 17 from the settler E are lifted 19 via a control valve c into the mixer F via a lift gas 18 (air) and mixed with the high temperature solids-laden synthesis gas 31 from the gasifier G for heat exchange. The heat exchange section adopts a turbulent fluid bed type. The gas after heat exchange enters a gas-solid separator Y-3 after passing through an upper solid sedimentation section to form 27, and the synthesis gas 28 after most of solid fine powder is separated out is sent out to be used as a product; the solid fines 29 are returned to the mixer F. The solid material 20 from the mixer is lifted to the carbonization pre-reactor C through the lifting gas 21 via the regulating valve D, the solid material 22 from the mixer is transferred to the cracking pre-reactor D through the regulating valve e, and the solid material 30 from the mixer is transferred to the gasifier G through the regulating valve f. The gas-solid separator Y-3 adopts a two-stage cyclone separator and is arranged at the top of the mixer F.

Shale semicoke 30 from the mixer F is controlled to enter the gasifier G through the regulating valve F to carry out gasification reaction with oxygen-containing gas 37 (pure oxygen and steam) passing through the gas distributor X-3, so as to obtain shale semicoke 32 and solid-containing synthetic gas 31.

Shale semicoke 32 from gasifier G is controlled by control valve G to enter burner H to react with oxygen-containing gas 39 (air) passing through gas distributor X-4 to release heat, resulting in calcined shale ash 34 and solids-containing gas 33.

The calcined shale ash 34 discharged from the burner H enters the heat collector I for heat recovery as shale ash product 35. The heat collector adopts primary heat collection, secondary heat collection and tertiary heat collection. The cooling medium used by the heat collector is deoxidized water.

The lifting gas 21 is dry gas, and the lifting gas 23 is dry gas.

The high-temperature oil gas 11 from the second-stage gas-solid separator Y-2 after most of the solids are separated is sent to the quenching device J and cooled by the quenching oil 47 separated from the washing device K.

The scrubber K is divided into an upper section and a lower section. The mixture 41 of quenching oil and oil gas enters the lower section of the scrubber, and the oil gas is in countercurrent contact with the scrubbing oil 45 from M in the ascending process of the lower section of the scrubber to carry out gas-liquid separation and further remove dust. The lower section of the scrubber is provided with a scrubbing liquid distribution structure and a herringbone baffle plate to improve the structure of countercurrent gas-liquid contact. The solid-containing heavy oil 42 separated from the lower section of the scrubber K is subjected to liquid-solid separation in the liquid-solid separator L, the separated low solid-containing heavy oil 43 enters the heat exchanger M to exchange heat and then returns to the scrubber K as washing oil to be subjected to countercurrent gas-liquid separation and dust removal with the mixture entering the bottom of the scrubber K, the low solid-containing heavy oil 46 after heat exchange can also be sent out as a product, and the high solid-containing heavy oil 44 separated by the liquid-solid separator L is returned to the carbonization pre-reactor C to be refined. The oil 49 pumped from the middle part of the scrubber returns to the upper part of the scrubber after passing through the heat exchanger N, and is subjected to secondary countercurrent gas-liquid separation and dust removal with the oil gas entering the upper part of the scrubber F, and a scrubbing liquid distribution structure and a structure for improving gas-liquid countercurrent contact by a separation tray are arranged at the upper section of the scrubber. The clean oil gas 52 after the heavy oil is separated by two-stage separation and washing is sent out from the top of the washer, and the clean oil product and clean dry gas can be separated subsequently.

The main operating conditions are:

the dry distillation reactor A has the following operating conditions: the pressure is 0.25-0.35 MPa (G), the temperature is 520-550 ℃, and the gas linear velocity is 0.8-1.2 m/s;

the operation conditions of the carbonization pre-reactor C are as follows: the pressure is 0.25-0.35 MPa (G), the temperature is 540-580 ℃, and the gas linear velocity is 0.6-1.0 m/s;

the cracking reactor B operating conditions were: the pressure is 0.25-0.35 MPa (G), the temperature is 480-520 ℃, and the gas linear velocity is 0.8-1.2 m/s;

the cracking prereactor D operating conditions were: the pressure is 0.25-0.35 MPa (G), the temperature is 560-600 ℃, and the gas linear velocity is 0.6-1.0 m/s;

the operating conditions of the settler E were: the pressure is 0.25-0.35 MPa (G), the temperature is 480-550 ℃, and the gas linear velocity is 0.1-0.3 m/s;

the mixer F operating conditions were: the pressure is 0.25-0.35 MPa (G), the temperature is 600-630 ℃, and the gas is

The body line speed is 0.2-0.5 m/s;

the gasifier G operating conditions were: the pressure is 0.25-0.35 MPa (G), the temperature is 950-980 ℃, and the gas linear velocity is 0.7-1.2 m/s.

The burner H operating conditions were: the pressure is 0.3-0.4 MPa (G), the temperature is 980-1050 ℃, and the gas linear velocity is 0.7-1.2 m/s;

the operating conditions of the heat collector are as follows: the pressure is 0.15-1.5 MPa, and the temperature is 80-950 DEG C

The quench cooler J operating conditions were: the pressure is 0.2-0.3 MPa (G), the temperature is 400-450 ℃, and the gas linear velocity is 8-20 m/s;

The operating conditions of the scrubber K are: the pressure is 0.15-0.25 MPa (G), the temperature is 120-380 ℃, and the upper gas linear velocity is 0.5-1 m/s;

the operating conditions of the heat exchanger M are: the pressure is 0.1-1.5 MPa, and the temperature is 120-340 ℃;

the operating conditions of the heat exchanger N are: the pressure is 0.1-1.5 MPa, and the temperature is 105-250 ℃;

the operating conditions of the liquid-solid separator L are as follows: the pressure is 0.1-1.0 MPa, and the temperature is 250-380 ℃;

the linear speed of the inlet of the gas-solid separator Y-1 is 15-22 m/s;

the linear speed of the inlet of the gas-solid separator Y-2 is 18-25 m/s;

the linear speed of the inlet of the gas-solid separator Y-3 is 18-25 m/s;

the length of the carbonization reactor A is 6-10 meters; />

The length of the carbonization pre-reactor C is 5-8 meters;

the length of the cracking reactor B is 6-10 m;

the length of the carbonization pre-reactor D is 5-8 meters;

the length of the settler E is 25-30 m;

the length of the heater F is 20-25 meters;

the length of the gasifier G is 15-20 meters;

the length of the burner H is 12-15 meters;

the length of the scrubber K is 28-32 meters.

(2) Product distribution:

TABLE 3 product distribution

Remarks: the solid heavy oil is completely recycled, and the solid heavy oil and the middle extraction oil are not produced. (3) the main properties of the product:

TABLE 4 major composition of the oil and gas (C4 below) products

Name of the name	Volume percent	Remarks
			Hydrogen gas	40.5％
Methane	21.3％
			Ethane (ethane)	10.2％
Ethylene	5.8％
			Propane	9.3％
Propylene	4.7％
			Carbon four	6.8％
Carbon dioxide	1.5％
			Carbon monoxide	0.4％

TABLE 5 simulated distillation data for oil and gas (C4 above) products

Weight percent	Distillation temperature (. Degree. C.)	Remarks
			5％	80
10％	125
			30％	205
50％	290
			70％	330
90％	390
			95％	425

TABLE 6 major composition of syngas

TABLE 7 shale ash main chemical composition

Name of the name	Weight percent	Remarks
			SiO ₂	52.2％
Al ₂ O ₃	21.3％
			Fe ₂ O ₃	8.7％
CaO	5.3％
			MgO	2.2％

All documents mentioned in this disclosure are incorporated by reference in this disclosure as if each were individually incorporated by reference. Further, it will be appreciated that various changes and modifications may be made by those skilled in the art after reading the above teachings, and such equivalents are intended to fall within the scope of the application as defined in the appended claims.

Claims

1. A comprehensive utilization method of heavy inferior oil and oil shale is characterized in that: comprising the following steps:

providing a comprehensive utilization device; the comprehensive utilization device is provided with a carbonization reactor (A), a carbonization pre-reactor (C), a cracking reactor (B), a cracking pre-reactor (D), a settler (E), a mixer (F), a gasifier (G), a combustor (H), a heat collector (I), a quencher (J) and a scrubber (K);

the settler (E) is provided with a settling section and a stripping section from top to bottom; comprises a first-stage gas-solid separator (Y-1), a second-stage gas-solid separator (Y-2) and a gas distributor (X-1); the primary gas-solid separator (Y-1) is arranged at the upper part of the interior of the settler (E); the secondary gas-solid separator (Y-2) is arranged inside or outside the settler (E); the gas distributor (X-1) is arranged at the lower part inside the settler (E);

The mixer (F) is provided with a mixing section and a stripping section at the upper part and the lower part; comprises a gas-solid separator (Y-3) and a mixer gas distributor (X-2); the gas-solid separator (Y-3) is arranged inside or outside the mixer (F); the mixer gas distributor (X-2) is arranged at the lower part inside the mixer (F);

the gasifier (G) is provided with a gasification section and a stripping section at the upper part and the lower part; comprises a gasifier gas distributor (X-3); the gasifier gas distributor (X-3) is arranged at the lower part inside the gasifier (G);

the burner (H) is provided with a combustion section and a stripping section at the upper part and the lower part; comprising a burner gas distributor (X-4); the burner gas distributor (X-4) is arranged at the lower part inside the burner (H);

wherein, the outlet of the carbonization reactor is connected with a first-stage gas-solid separator in the settler, and the inlet is connected with the carbonization pre-reactor; the outlet of the cracking reactor is connected with the settler, and the inlet of the cracking reactor is connected with the cracking pre-reactor; the upper outlet of the settler is connected with a quencher, and the lower outlet of the settler is respectively connected with a carbonization pre-reactor, a cracking pre-reactor and a mixer; the upper part of the mixer is provided with an outlet, and the lower outlet is respectively connected with a carbonization pre-reactor, a cracking pre-reactor and a gasifier; the upper outlet of the gasifier is connected with a mixer gas distributor at the lower part of the mixer, and the lower outlet is connected with a burner; the lower outlet of the burner is connected with the inlet of the heat collector, and the upper outlet of the burner is connected with the inlet of the gasifier; the inlet of the quenching device is connected with a secondary gas-solid separator in the settler, and the outlet of the quenching device is connected with the bottom inlet of the scrubber; the upper part of the scrubber is respectively provided with an outlet connected with the quenching device and the cracking pre-reactor;

The comprehensive utilization method further comprises the following steps:

2. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the method comprises the following steps: the comprehensive utilization device is also provided with a liquid-solid separator (L) and a heavy oil heat exchanger (M); wherein, the outlet of the bottom of the scrubber is connected with the inlet of the liquid-solid separator; the outlet of the liquid-solid separator is respectively connected with the inlet of the carbonization pre-reactor and the heavy oil heat exchanger; the outlet of the heavy oil heat exchanger is connected with the inlet of the middle part of the scrubber.

3. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the method comprises the following steps: the comprehensive utilization device is also provided with an oil extraction heat exchanger (N); wherein, the inlet and outlet of the oil extraction heat exchanger are respectively connected with the middle part and the upper part of the scrubber.

4. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, further comprising the steps of: the mixed oil gas from the settler enters a scrubber after passing through a quencher, and solid-containing heavy oil separated from the bottom of the scrubber is sent to a liquid-solid separator for liquid-solid separation; the separated low-solid-content heavy oil is returned to the scrubber as washing liquid or sent out as a product after heat exchange by a heavy oil heat exchanger; the separated high-solid-content heavy oil enters a carbonization pre-reactor to carry out secondary carbonization reaction;

5. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, further comprising the steps of: part of the extracted oil flowing out of the middle part of the scrubber is heated by the extracted oil heat exchanger and then returned to the scrubber to be used as a scrubbing liquid or sent out as a product.

6. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the heavy inferior oil raw material is a flowing substance containing hydrocarbon; wherein the flowable substance is selected from one or more of the following group: heavy oil, residual oil, tar, slurry oil, swill-cooked dirty oil, waste oil, dirty oil and shale oil; the solids content of the flowable substance is less than 15% by weight.

7. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the grain size of the oil shale raw material is not more than 8 mm.

8. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the oil shale raw material can be mixed with hydrocarbon-containing solid substances; wherein the hydrocarbon-containing solid material is selected from one or more of the following group: lignite, bituminous coal with a caking index gr.i. <50, long flame coal, anthracite, sludge, and oil sludge; the grain diameter of the solid matters containing hydrocarbon is less than or equal to 8 mm; the proportion of the hydrocarbon-containing solid matter is less than or equal to 50% by weight.

9. The method for comprehensively utilizing heavy inferior oil and oil shale according to claim 1, wherein the proportion of the heavy inferior oil raw material to the oil shale raw material is as follows: 5%:95% -95%: 5% by weight.