Method and system for utilizing petroleum coke volatile components and flue gas generated after petroleum coke calcination

Abstract

The invention relates to the technical field of waste gas recycling in the calcination link of carbon petroleum coke for aluminum, in particular to a method and system for utilizing petroleum coke volatile components and flue gas generated after petroleum coke calcination. The method comprises the following steps: cooling flue gas after calcining petroleum coke, and then carrying out carbon dioxide adsorption to obtain a carbon dioxide component; the method comprises the following steps: calcining petroleum coke to remove volatile components of the petroleum coke to obtain pretreated petroleum coke volatile components with hydrogen and methane; carrying out heat exchange on the pretreated petroleum coke volatile component to obtain a volatile component raw material; carrying out catalytic reaction on the carbon dioxide component and the volatile component raw material to obtain a methanol product; wherein the volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material meet the relational expression: V1: V2 = (1: 2)-(1: 4). According to the method, the petroleum coke volatile component and the flue gas after calcining the petroleum coke can be used as raw materials and are subjected to catalytic reaction to obtain a methanol product, so that the recycling rate of the petroleum coke volatile component and the flue gas after calcining the petroleum coke is increased.

Description

Technical Field

[0001] The present application relates to the technical field of waste gas recovery and utilization during the calcination of petroleum coke for aluminum, and in particular to a method and system for the coordinated recycling of petroleum coke volatiles and flue gas after calcination of petroleum coke. Background Art

[0002] Petroleum coke is an important raw material for carbon anode production. At present, petroleum coke accounts for more than 80% of the weight of carbon anode. Therefore, the quality of petroleum coke has a great influence on various indicators of carbon anode. In the production of carbon anode, petroleum coke needs to be calcined at high temperature to remove moisture and volatiles in petroleum coke, and to improve the density, mechanical strength, electrical conductivity, chemical stability and antioxidant properties of petroleum coke. At present, the main equipment for calcining petroleum coke includes rotary kiln, pot calciner and rotary bed, etc. However, the amount of volatile matter in petroleum coke has a great influence on the calcining process of petroleum coke. For example, when calcining petroleum coke in rotary kiln or pot furnace, if the volatile matter content in petroleum coke is at a low level (<8%), the thermal treatment of petroleum coke calcination will have problems such as insufficient heat source, low degree of coke heat treatment after calcination of petroleum coke and low flue gas temperature; if the volatile matter content in petroleum coke is at a high level (>12%), the thermal treatment of petroleum coke calcination will precipitate more volatile matter, which will greatly affect the temperature system, calcination equipment, waste heat utilization, desulfurization system and other links of petroleum coke calcination. However, the volatile matter of petroleum coke in different origins and at different times fluctuates greatly. Generally, the content of volatile matter in petroleum coke is distributed between 7% and 16%, which has caused great trouble to the thermal treatment of petroleum coke calcination. Current research has found that the main components of petroleum coke volatiles are gases such as H2 and CH4, among which the sum of the weights of CH4 and H2 accounts for about 91% to 95% of the total weight of petroleum coke volatiles.

[0003] When the content of volatile matter in petroleum coke is greater than 11%, a large amount of volatile matter will be produced, which is not conducive to the temperature control of petroleum coke calcination, and will also cause the temperature of the material to be too high when it is discharged, thereby affecting the quality of the calcined petroleum coke. This will undoubtedly seriously restrict the quality improvement and production increase of petroleum coke calcination, as well as the utilization of waste heat from petroleum coke calcination and the environmental protection management of petroleum coke calcination. In addition, the calcination process of petroleum coke will produce a large amount of high-temperature flue gas, the components of which are mainly CO2, SO2, NO x At present, high-temperature flue gas is mainly recycled by preheating and power generation. However, at present, the excess petroleum coke volatiles and high-temperature flue gas in the petroleum coke calcination process are mainly directly burned, and it is difficult to effectively recycle the components therein. Summary of the invention

[0004] The present application provides a method and system for recycling petroleum coke volatiles and flue gas after petroleum coke calcination to solve the following technical problem: how to improve the recovery rate of petroleum coke volatiles and high-temperature flue gas generated in the petroleum coke calcination process.

[0005] In a first aspect, the present application provides a method for utilizing petroleum coke volatiles and flue gas after calcination of petroleum coke, wherein the petroleum coke volatiles include hydrogen, methane and tar, and the flue gas after calcination includes carbon dioxide and nitrogen oxides, and the method comprises:

[0006] The petroleum coke flue gas is cooled and then subjected to carbon dioxide adsorption to obtain a carbon dioxide component;

[0007] calcining the petroleum coke volatiles to remove the volatiles of the petroleum coke and obtain pretreated petroleum coke volatiles containing hydrogen and methane;

[0008] Exchanging heat with the pretreated petroleum coke volatile matter containing hydrogen and methane to obtain a volatile matter raw material containing hydrogen and methane;

[0009] Catalyzing the carbon dioxide component and the volatile raw material containing hydrogen and methane to promote the carbon dioxide component and the hydrogen and methane in the volatile raw material to react to generate methanol, thereby obtaining a methanol product;

[0010] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=(1:2)-(1:4).

[0011] Optionally, the temperatures of the volatile raw material and the carbon dioxide component are 200° C. to 300° C. respectively.

[0012] Optionally, the end point temperature of the cooling is 200°C to 300°C.

[0013] Optionally, the temperature of the catalytic reaction is 250° C. to 300° C., and the time of the catalytic reaction is 2 h to 5 h.

[0014] Optionally, the pressure of the catalytic reaction is 5 MPa to 10 MPa.

[0015] Optionally, the calcining of the petroleum coke volatiles to remove the volatiles of the petroleum coke to obtain pretreated petroleum coke volatiles containing hydrogen and methane comprises the following steps:

[0016] The petroleum coke volatiles are calcined, and then the calcined petroleum coke volatiles are washed and cooled to remove tar volatiles from the petroleum coke volatiles, thereby obtaining pretreated petroleum coke volatiles containing hydrogen and methane.

[0017] Optionally, the cooling end point temperature is 200°C to 300°C.

[0018] Optionally, the heat of the heat exchange comes from the heat of the cooling.

[0019] In a second aspect, the present application provides a system for utilizing petroleum coke volatile matter and flue gas after petroleum coke calcination, the system being adapted to the method described in the first aspect, the system being connected to the outlet of the petroleum coke calcination equipment, and the system comprising:

[0020] The petroleum coke volatile matter processing part comprises a volatile matter scrubber, a gas storage device and a heat medium jacket, wherein the feed port of the volatile matter scrubber is connected to the volatile matter outlet of the petroleum coke calcining equipment, the discharge port of the volatile matter scrubber is connected to the feed port of the gas storage device, and the heat medium jacket is wrapped around the surface of the gas storage device;

[0021] A flue gas treatment unit after petroleum coke calcination, comprising a heat medium boiler and a carbon dioxide adsorption device, wherein the feed port of the heat medium boiler is connected to the flue gas outlet of the petroleum coke calcination equipment, the heat medium boiler is connected to the heat medium jacket, and the discharge port of the heat medium boiler is connected to the feed port of the carbon dioxide adsorption device;

[0022] The methanol synthesis unit comprises a flow control unit and a methanol synthesis tower. The feed port of the flow control unit is respectively connected to the discharge port of the gas storage device and the discharge port of the carbon dioxide adsorption device, and the methanol synthesis tower is connected to the discharge port of the flow control unit.

[0023] Optionally, the flow control unit includes a volatile matter flow control valve and a carbon dioxide flow control valve, the feed port of the volatile matter flow control valve is connected to the discharge port of the gas storage device, and the feed port of the carbon dioxide flow control valve is connected to the discharge port of the carbon dioxide adsorption device.

[0024] The above technical solution provided by the embodiment of the present application has the following advantages compared with the prior art:

[0025] A method for utilizing petroleum coke volatiles and flue gas after calcination of petroleum coke is provided in an embodiment of the present application. The method first cools the flue gas after calcination of petroleum coke and performs carbon dioxide adsorption treatment to separate pure carbon dioxide components from the flue gas after calcination of petroleum coke, and further removes and exchanges heat on the petroleum coke volatiles to obtain a volatile raw material containing only hydrogen and methane. The volatile raw material and the carbon dioxide component are then mixed and then subjected to a catalytic reaction. During the catalytic reaction, the hydrogen and methane in the volatile raw material react fully with the carbon dioxide component to generate methanol. In addition, the volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=(1:2)~(1:4), so as to further promote the carbon dioxide component to react fully with the hydrogen and methane in the volatile raw material and generate a sufficient amount of methanol product. This shows that the method uses petroleum coke volatiles and flue gas after calcination of petroleum coke as raw materials and obtains methanol products through a catalytic reaction, so that the recovery rate of petroleum coke volatiles and flue gas after calcination of petroleum coke can be improved by this method. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present application and, together with the description, serve to explain the principles of the present application.

[0027] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative labor.

[0028] Figure 1 A schematic flow chart of a method for utilizing petroleum coke volatile matter and flue gas after calcining petroleum coke provided in an embodiment of the present application;

[0029] Figure 2 A detailed schematic diagram of a method for utilizing petroleum coke volatile matter and flue gas after calcination of petroleum coke provided in an embodiment of the present application;

[0030] Figure 3 A system logic diagram for utilizing petroleum coke volatile matter and flue gas after calcination of petroleum coke provided in an embodiment of the present application;

[0031] Figure 4 The actual structure diagram of a system for utilizing petroleum coke volatile matter and flue gas after calcination of petroleum coke provided in the embodiment of the present application;

[0032] Among them, 1-petroleum coke calcining equipment, 101-volatile matter avenue, 102-volatile matter collecting hole, 103-high-temperature flue gas outlet, 2-volatile matter scrubber, 3-gas storage device, 4-heat medium jacket, 5-heat medium boiler, 6-carbon dioxide adsorption device, 7-flow control unit, 71-volatile matter flow control valve, 72-carbon dioxide flow control valve, 8-methanol synthesis tower. DETAILED DESCRIPTION

[0033] In order to make the purpose, technical solution and advantages of the embodiments of the present application clearer, the technical solution in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of this application.

[0034] Various embodiments of the present application may be presented in the form of a range; it should be understood that the description in the form of a range is only for convenience and brevity and should not be understood as a rigid limitation on the scope of the present application; therefore, it should be considered that the range description has specifically disclosed all possible sub-ranges and single numerical values ​​within the range; for example, it should be considered that the range description from 1 to 6 has specifically disclosed sub-ranges, such as from 1 to 3, from 1 to 4, from 1 to 5, from 2 to 4, from 2 to 6, from 3 to 6, etc., as well as single numbers within the range, such as 1, 2, 3, 4, 5 and 6, which applies regardless of the range; in addition, whenever a numerical range is indicated in this document, it is meant to include any cited numbers (fractions or integers) within the indicated range.

[0035] In this document, the terms "including" and "comprising" mean "including but not limited to". Unless otherwise specified, various raw materials, reagents, instruments and equipment used in this application can be purchased from the market or prepared by existing methods.

[0036] Figure 1 A schematic flow chart of a method for utilizing volatile matter from petroleum coke and flue gas after calcination of petroleum coke provided in an embodiment of the present application is shown by way of example;

[0037] like Figure 1 As shown, the embodiment of the present application provides a method for utilizing petroleum coke volatiles and flue gas after calcination of petroleum coke, wherein the composition of the petroleum coke volatiles includes hydrogen, methane and tar, and the flue gas after calcination includes carbon dioxide and nitrogen oxides, and the method includes:

[0038] S1. Cooling the flue gas after calcining petroleum coke, and then adsorbing carbon dioxide to obtain a carbon dioxide component;

[0039] S2. calcining the petroleum coke volatiles to remove the volatiles of the petroleum coke to obtain pretreated petroleum coke volatiles having hydrogen and methane;

[0040] S3. exchanging heat with the pretreated petroleum coke volatiles having hydrogen and methane to obtain a volatile raw material having hydrogen and methane;

[0041] S4. catalyzing the carbon dioxide component and the volatile raw material having hydrogen and methane to promote the carbon dioxide component and the hydrogen and methane in the volatile raw material to react to produce methanol to obtain a methanol product;

[0042] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=(1:2)-(1:4).

[0043] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:2, 1:2.5, 1:3, 1:3.5 or 1:4.

[0044] It should be noted that the main component of the flue gas after the petroleum coke is calcined is carbon dioxide gas, and the volume of the carbon dioxide can be greater than 20% of the total volume of the flue gas after the petroleum coke is calcined.

[0045] It should be noted that the main components of the petroleum coke volatile matter are hydrogen and methane, the volume of the hydrogen can be greater than 50% of the total volume of the petroleum coke volatile matter, and the volume of the methane can be greater than 40% of the total volume of the petroleum coke volatile matter.

[0046] In some optional embodiments, the temperature of the volatile raw material and the carbon dioxide component is 200° C. to 300° C. respectively;

[0047] In these embodiments, the temperature of the volatile raw material and the carbon dioxide component can be 200°C to 300°C, respectively, which can promote sufficient temperature for catalytic reaction between hydrogen and methane in the volatile raw material and the carbon dioxide component and generate sufficient methanol product. This means that petroleum coke volatiles and flue gas after calcining petroleum coke can be used as raw materials and methanol products can be obtained through catalytic reaction, so that the recovery rate of petroleum coke volatiles and flue gas after calcining petroleum coke can be improved through this method.

[0048] The temperature of the volatile feed and the carbon dioxide component may be 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C or 300°C, respectively.

[0049] In some optional embodiments, the end point temperature of the cooling is 200°C to 300°C;

[0050] In these embodiments, the terminal temperature of the cooling can be 200°C to 300°C, which can enable the carbon dioxide component to have sufficient temperature to catalytically react with hydrogen and methane in the volatile raw materials and generate a sufficient amount of methanol product, indicating that petroleum coke volatiles and flue gas after petroleum coke calcination can be used as raw materials and catalytically react to generate methanol products, thereby improving the recovery and utilization rate of petroleum coke volatiles and flue gas after petroleum coke calcination through this method.

[0051] The end point temperature of the temperature reduction may be 210°C, 220°C, 230°C, 240°C, 250°C, 260°C, 270°C, 280°C, 290°C or 300°C.

[0052] In some optional embodiments, the temperature of the catalytic reaction is 250° C. to 300° C., and the time of the catalytic reaction is 2 h to 5 h.

[0053] In these embodiments, the temperature of the catalytic reaction can be 250°C to 300°C, and the time of the catalytic reaction can be 2h to 5h, which can promote the catalytic reaction between the carbon dioxide component and the hydrogen and methane in the volatile raw materials to fully react and generate a sufficient amount of methanol product, indicating that petroleum coke volatiles and flue gas after petroleum coke calcination can be used as raw materials and catalytically react to generate methanol products, thereby improving the recovery and utilization rate of petroleum coke volatiles and flue gas after petroleum coke calcination through this method.

[0054] The temperature of the catalytic reaction may be 250°C, 260°C, 270°C, 280°C, 290°C or 300°C.

[0055] The catalytic reaction time can be 2h, 3h, 4h, or 5h.

[0056] In some optional embodiments, the pressure of the catalytic reaction is 5 MPa to 10 MPa;

[0057] In these embodiments, the pressure of the catalytic reaction can be 5MPa to 10MPa, which can promote the catalytic reaction between the carbon dioxide component and the hydrogen and methane in the volatile raw materials to fully react and generate a sufficient amount of methanol product, indicating that petroleum coke volatiles and flue gas after petroleum coke calcination can be used as raw materials and catalytically react to generate methanol products, thereby improving the recovery and utilization rate of petroleum coke volatiles and flue gas after petroleum coke calcination through this method.

[0058] The pressure of the catalytic reaction can be 5 MPa, 6 MPa, 7 MPa, 8 MPa, 9 MPa or 10 MPa.

[0059] Figure 2 A detailed flow chart of a method for utilizing volatile matter of petroleum coke and flue gas after calcination of petroleum coke provided in an embodiment of the present application is exemplarily shown;

[0060] like Figure 2 As shown, in some optional embodiments, the calcining of petroleum coke volatiles to remove the volatiles of the petroleum coke to obtain pretreated petroleum coke volatiles having hydrogen and methane comprises the steps of:

[0061] S201. calcining the petroleum coke volatiles, and then washing and cooling the calcined petroleum coke volatiles to remove the volatiles of the petroleum coke volatiles to obtain pretreated petroleum coke volatiles having hydrogen and methane;

[0062] In these embodiments, the removal treatment may include washing and cooling. The polar gas components and non-polar tar impurities in the petroleum coke volatiles can be initially separated by washing, and then the non-polar tar and polar gas components can be further separated by cooling to obtain pure pretreated petroleum coke volatiles containing hydrogen and methane.

[0063] In some optional embodiments, the cooling end temperature is 200°C to 300°C;

[0064] In these embodiments, the cooling end temperature may be 200° C. to 300° C., and the non-polar tar and the polar gas components may be further separated by cooling to obtain pure pretreated petroleum coke volatiles containing hydrogen and methane.

[0065] The end point temperature of the cooling may be 200°C, 220°C, 240°C, 260°C, 280°C or 300°C.

[0066] In some optional embodiments, the heat of the heat exchange comes from the heat of the cooling;

[0067] In these embodiments, the heat for heat exchange can come from the heat for cooling, and the heat exchange heat of the flue gas after petroleum coke calcination can be used as a heat source to heat the pre-treated petroleum coke volatiles to facilitate the subsequent catalytic reaction, so as to improve the recovery rate of petroleum coke volatiles and flue gas after petroleum coke calcination through this method.

[0068] Figure 3 The following is a schematic diagram of a system logic for utilizing volatile matter of petroleum coke and flue gas after calcination of petroleum coke provided in an embodiment of the present application;

[0069] Figure 4 The actual structure diagram of a system using petroleum coke volatile matter and flue gas after calcination of petroleum coke provided in the embodiment of the present application is shown as an example

[0070] Based on a general inventive concept, such as Figure 3 and Figure 4As shown, the embodiment of the present application provides a system for utilizing petroleum coke volatile matter and flue gas after petroleum coke calcination, the system is adapted to the method, the system is connected to the outlet of the petroleum coke calcination equipment 1, and the system includes:

[0071] The petroleum coke volatile matter processing part comprises a volatile matter scrubber 2, a gas storage device 3 and a heat medium jacket 4, wherein the feed port of the volatile matter scrubber 2 is connected to the volatile matter outlet of the petroleum coke calcining equipment 1, the discharge port of the volatile matter scrubber 2 is connected to the feed port of the gas storage device 3, and the heat medium jacket 4 is wrapped around the surface of the gas storage device 3;

[0072] The petroleum coke calcined flue gas treatment unit comprises a heat medium boiler 5 and a carbon dioxide adsorption device 6, wherein the feed port of the heat medium boiler 5 is connected to the petroleum coke calcined flue gas outlet of the petroleum coke calcining equipment 1, the heat medium boiler 5 is connected to the heat medium jacket 4, and the discharge port of the heat medium boiler 5 is connected to the feed port of the carbon dioxide adsorption device 6;

[0073] The methanol synthesis section includes a flow control unit 7 and a methanol synthesis tower 8. The feed port of the flow control unit 7 is respectively connected to the discharge port of the gas storage device 3 and the discharge port of the carbon dioxide adsorption device 6. The methanol synthesis tower 8 is connected to the discharge port of the flow control unit 7.

[0074] The system is implemented based on the above method. The specific steps of the method can refer to the above embodiment. Since the system adopts part or all of the technical solutions of the above embodiment, it has at least all the beneficial effects brought by the technical solutions of the above embodiment, which will not be repeated here.

[0075] It should be noted that the petroleum coke calcining equipment 1 generally includes a volatile matter avenue 101 and volatile matter collecting holes 102 arranged around the volatile matter avenue 101. These volatile matter collecting holes 102 can collect petroleum coke volatiles in the volatile matter avenue 101, so as to obtain a sufficient amount of petroleum coke volatiles.

[0076] It should be noted that the petroleum coke calcining equipment 1 is generally provided with a high-temperature flue gas outlet 103, which can be used to export the high-temperature flue gas generated by the petroleum coke calcining. The high-temperature flue gas can first be controlled to have a temperature of 280°C to 320°C by waste heat power generation, thereby obtaining the flue gas after petroleum coke calcination.

[0077] It should be noted that a catalyst unit is provided in the methanol synthesis tower 8 to catalyze the reaction between the carbon dioxide component and the volatile raw material, thereby obtaining a large amount of methanol product.

[0078] In some optional embodiments, the flow control unit 7 includes a volatile matter flow control valve 71 and a carbon dioxide flow control valve 72, the feed port of the volatile matter flow control valve 71 is connected to the discharge port of the gas storage device 3, and the feed port of the carbon dioxide flow control valve 72 is connected to the discharge port of the carbon dioxide adsorption device 6;

[0079] In these embodiments, the flow control unit 7 may include a volatile matter flow control valve 71 and a carbon dioxide flow control valve 72, and the feed port of the volatile matter flow control valve 71 is connected to the discharge port of the gas storage device 3, and the feed port of the carbon dioxide flow control valve 72 is connected to the discharge port of the carbon dioxide adsorption device 6. The volatile matter flow control valve 71 and the carbon dioxide flow control valve 72 can be used to adjust the intake amount of the volatile matter raw material and the carbon dioxide component, respectively, so that the volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=(1:2)~(1:4), so that the petroleum coke volatile matter and the flue gas after the petroleum coke is calcined are used as raw materials and are catalytically reacted to generate methanol products, so that the recovery rate of the petroleum coke volatile matter and the flue gas after the petroleum coke is calcined can be improved through the system.

[0080] The present application is further described below in conjunction with specific examples. The experimental methods in the following examples that do not specify specific conditions are usually measured according to industry standards; if there are no corresponding industry standards, they are carried out according to common international standards, conventional conditions, or conditions recommended by the manufacturer.

[0081] Example 1

[0082] like Figure 1 and Figure 2 As shown, a method for utilizing petroleum coke volatiles and flue gas after calcination of petroleum coke, wherein the composition of the petroleum coke volatiles includes hydrogen, methane and tar, and the flue gas after calcination includes carbon dioxide and nitrogen oxides, including:

[0083] S1. Cooling the flue gas after calcining petroleum coke, and then adsorbing carbon dioxide to obtain a carbon dioxide component;

[0084] S201. The petroleum coke volatiles are calcined, and then the calcined petroleum coke volatiles are washed and cooled to remove the volatiles of the petroleum coke volatiles to obtain pretreated petroleum coke volatiles having hydrogen and methane;

[0085] S3. exchanging heat with the pretreated petroleum coke volatiles having hydrogen and methane to obtain a volatile raw material;

[0086] S4. The carbon dioxide component and the volatile raw material are mixed, and then subjected to a catalytic reaction to promote the carbon dioxide component and the hydrogen component in the volatile raw material to react to generate methanol to obtain a methanol product;

[0087] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:2.

[0088] The temperature of the volatile raw material was 260°C and the temperature of the carbon dioxide component was 250°C.

[0089] The end point temperature of the cooling is 280°C.

[0090] The catalytic reaction temperature is 250°C and the catalytic reaction time is 5h.

[0091] The pressure of the catalytic reaction is 5 MPa.

[0092] Example 2

[0093] Based on the method disclosed in Example 1, a corresponding system is further designed, as follows:

[0094] like Figure 3 As shown, a system utilizing petroleum coke volatile matter and flue gas after petroleum coke calcination is adapted to the method disclosed in Example 1, the system is connected to the outlet of the petroleum coke calcination equipment 1, and the system includes:

[0095] The petroleum coke volatile matter processing part includes a volatile matter scrubber 2, a gas storage device 3 and a heat medium jacket 4, the feed port of the volatile matter scrubber 2 is connected to the volatile matter outlet of the petroleum coke calcining equipment 1, the discharge port of the volatile matter scrubber 2 is connected to the feed port of the gas storage device 3, and the heat medium jacket 4 is wrapped around the surface of the gas storage device 3;

[0096] The flue gas treatment section after petroleum coke calcination includes a heat medium boiler 5 and a carbon dioxide adsorption device 6, wherein the feed port of the heat medium boiler 5 is connected to the flue gas outlet of the petroleum coke calcination equipment 1, the heat medium boiler 5 is connected to the heat medium jacket 4, and the discharge port of the heat medium boiler 5 is connected to the feed port of the carbon dioxide adsorption device 6;

[0097] The methanol synthesis section includes a flow control unit 7 and a methanol synthesis tower 8. The feed port of the flow control unit 7 is connected to the discharge port of the gas storage device 3 and the discharge port of the carbon dioxide adsorption device 6 respectively, and the methanol synthesis tower 8 is connected to the discharge port of the flow control unit 7.

[0098] The flow control unit 7 includes a volatile matter flow control valve 71 and a carbon dioxide flow control valve 72 . The feed port of the volatile matter flow control valve 71 is connected to the discharge port of the gas storage device 3 , and the feed port of the carbon dioxide flow control valve 72 is connected to the discharge port of the carbon dioxide adsorption device 6 .

[0099] Example 3

[0100] Based on the contents disclosed in Example 1, the following modifications are further made:

[0101] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:3.

[0102] The temperature of the volatile raw material was 270°C and the temperature of the carbon dioxide component was 260°C.

[0103] The end point temperature of the cooling is 280°C.

[0104] The catalytic reaction temperature is 270°C and the catalytic reaction time is (3) h.

[0105] The pressure of the catalytic reaction is 8 MPa.

[0106] Example 4

[0107] Based on the contents disclosed in Example 1, the following modifications are further made:

[0108] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:4.

[0109] The temperature of the volatile raw material was 300°C and the temperature of the carbon dioxide component was 270°C.

[0110] The end point temperature of the cooling is 300°C.

[0111] The temperature of the catalytic reaction is 280°C and the catalytic reaction time is 2h.

[0112] The pressure of the catalytic reaction is 5 MPa.

[0113] Comparative Example 1

[0114] Based on the contents disclosed in Example 1, the following modifications are further made:

[0115] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:1.

[0116] Comparative Example 2

[0117] Based on the contents disclosed in Example 1, the following modifications are further made:

[0118] The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=1:5.

[0119] Comparative Example 3

[0120] Based on the contents disclosed in Example 1, the following modifications are further made:

[0121] The temperature of the volatile raw material was 220°C and the temperature of the carbon dioxide component was 200°C.

[0122] The catalytic reaction temperature is 200°C and the catalytic reaction time is 5.

[0123] Comparative Example 4

[0124] Based on the contents disclosed in Example 1, the following modifications are further made:

[0125] The temperature of the volatile raw material was 350°C and the temperature of the carbon dioxide component was 320°C.

[0126] The catalytic reaction temperature is 340°C and the catalytic reaction time is 2.

[0127] Comparative Example 5

[0128] Based on the contents disclosed in Example 1, the following modifications are further made:

[0129] The pressure of the catalytic reaction is 2 MPa.

[0130] Comparative Example 6

[0131] Based on the contents disclosed in Example 1, the following modifications are further made:

[0132] The pressure of the catalytic reaction is 15 MPa.

[0133] Related experiments and effect data:

[0134] The conversion rates of petroleum coke volatile matter and flue gas after calcination of petroleum coke in the methanol products obtained by the methods of Example 1, Example 3 and Example 4 and Comparative Examples 1 to Comparative Examples 6 were respectively counted, and the results are shown in Table 1.

[0135] Table 1 Conversion rate of petroleum coke volatile matter and flue gas after petroleum coke calcination in methanol products obtained in various embodiments and comparative examples

[0136]

[0137] As can be seen from Table 1, the method for utilizing petroleum coke volatiles and flue gas after calcination of petroleum coke provided in the embodiment of the present application can use petroleum coke volatiles and flue gas after calcination of petroleum coke as raw materials and obtain a methanol product through a catalytic reaction to improve the recovery rate of petroleum coke volatiles and flue gas after calcination of petroleum coke.

[0138] In addition, an embodiment of the present application provides a method for utilizing petroleum coke volatiles and flue gas after calcining petroleum coke, which produces methanol through green chemical reactions from calcining petroleum coke and flue gas after calcining petroleum coke, and can improve the efficient recovery and utilization of flue gas after calcining petroleum coke and petroleum coke volatiles.

[0139] In addition, a system for utilizing petroleum coke volatiles and flue gas after calcining petroleum coke provided in an embodiment of the present application can stabilize the operation of the petroleum coke calcining furnace to improve the quality of calcined petroleum coke. In addition, the system can achieve efficient utilization of excess volatiles and high-temperature flue gas of petroleum coke, and can replace traditional fossil energy in some fields.

[0140] The above is only a specific implementation of the present application, so that those skilled in the art can understand or implement the present application. It will be apparent to those skilled in the art that various modifications to these embodiments are possible, and the general principles defined in the present application can be implemented in other embodiments without departing from the spirit or scope of the present application. Therefore, the present application will not be limited to these embodiments shown in the present application, but will conform to the widest scope consistent with the principles and novel features applied for by the present application.

Claims

1. A method for utilizing petroleum coke volatile matter and flue gas after calcination of petroleum coke, characterized in that: The petroleum coke volatile matter comprises hydrogen, methane and tar, the calcined flue gas comprises carbon dioxide and nitrogen oxides, and the method comprises: The flue gas after calcining petroleum coke is cooled, and then carbon dioxide is adsorbed to obtain a carbon dioxide component; calcining the petroleum coke volatiles to remove the volatiles of the petroleum coke and obtain pretreated petroleum coke volatiles containing hydrogen and methane; exchanging heat with the pretreated petroleum coke volatile matter containing hydrogen and methane to obtain a volatile matter raw material containing hydrogen and methane; Catalyzing the carbon dioxide component and the volatile raw material containing hydrogen and methane to promote the carbon dioxide component and the hydrogen and methane in the volatile raw material to react to generate methanol, thereby obtaining a methanol product; The volume V1 of the carbon dioxide component and the volume V2 of the volatile raw material satisfy the relationship: V1:V2=(1:2)-(1:4).

2. The method according to claim 1, characterized in that: The temperatures of the volatile raw material and the carbon dioxide component are 200° C. to 300° C. respectively.

3. The method according to claim 1, characterized in that The terminal temperature of the cooling is 200°C to 300°C.

4. The method according to claim 1, characterized in that: The temperature of the catalytic reaction is 250° C. to 300° C., and the time of the catalytic reaction is 2 h to 5 h.

5. The method according to claim 1, characterized in that The pressure of the catalytic reaction is 5MPa to 10MPa.

6. The method according to claim 1, characterized in that The calcining of petroleum coke volatiles to remove the volatiles of the petroleum coke to obtain pretreated petroleum coke volatiles containing hydrogen and methane comprises the following steps: The petroleum coke volatiles are calcined, and then the calcined petroleum coke volatiles are washed and cooled to remove the volatiles of the petroleum coke volatiles, thereby obtaining pretreated petroleum coke volatiles containing hydrogen and methane.

7. The method according to claim 6, characterized in that The terminal temperature of the cooling is 200°C to 300°C.

8. The method according to claim 1, characterized in that The heat of heat exchange comes from the heat of cooling.

9. A system for utilizing volatile matter from petroleum coke and flue gas from calcined petroleum coke, characterized in that: The system is adapted to the method according to any one of claims 1 to 8, the system is connected to the outlet of the petroleum coke calcining device (1), and is characterized in that the system comprises: A petroleum coke volatile matter processing section comprises a volatile matter scrubber (2), a gas storage device (3) and a heat medium jacket (4), wherein the feed port of the volatile matter scrubber (2) is connected to the volatile matter outlet of the petroleum coke calcining equipment (1), the discharge port of the volatile matter scrubber (2) is connected to the feed port of the gas storage device (3), and the heat medium jacket (4) is wrapped around the surface of the gas storage device (3); A flue gas treatment section after petroleum coke calcination comprises a heat medium boiler (5) and a carbon dioxide adsorption device (6), wherein the feed port of the heat medium boiler (5) is connected to the flue gas outlet of the petroleum coke calcination equipment (1), the heat medium boiler (5) is connected to the heat medium jacket (4), and the discharge port of the heat medium boiler (5) is connected to the feed port of the carbon dioxide adsorption device (6); The methanol synthesis section comprises a flow control unit (7) and a methanol synthesis tower (8), wherein the feed port of the flow control unit (7) is respectively connected to the discharge port of the gas storage device (3) and the discharge port of the carbon dioxide adsorption device (6), and the methanol synthesis tower (8) is connected to the discharge port of the flow control unit (7).

10. The system according to claim 9, characterized in that The flow control unit (7) comprises a volatile matter flow control valve (71) and a carbon dioxide flow control valve (72); the feed port of the volatile matter flow control valve (71) is connected to the discharge port of the gas storage device (3), and the feed port of the carbon dioxide flow control valve (72) is connected to the discharge port of the carbon dioxide adsorption device (6).

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