Method for treating waste residue and oil sludge in coordination

Abstract

The present disclosure relates to a method for treating gasification waste residue and oil sludge, wherein the gasification waste residue is obtained after preparing synthesis gas from heavy oil-based raw materials, and the method comprises the following steps: S1, uniformly mixing the gasification waste residue and oil sludge residue to form a first mixture; the oil sludge residue is obtained after dehydrating and deoiling the oil sludge; S2, burning and decarburizing the first mixture. The method makes the decarburization of the gasification waste residue more efficient and sufficient, which is conducive to the economic recovery of vanadium and / or nickel resources in the gasification waste residue; at the same time, the residual organic matter in the oil sludge residue is completely burned and removed, and the oil sludge is completely reduced.

Description

Technical Field

[0001] This disclosure relates to the field of solid waste treatment technology, and more specifically, to a method for the co-treatment of gasification waste residue and oil sludge. Background Technology

[0002] During the partial oxidation reaction of heavy petroleum-based feedstocks (residue oil, deoiled bitumen, petroleum coke) with gasifying agents (oxygen, steam) to generate syngas under high temperature and high pressure, a large amount of fine-particle, high-carbon waste residue (also known as "carbon black" or "carbon black waste residue") is produced. In recent years, in order to adapt to cleaner production and improve the utilization rate of petroleum resources, refineries have been actively adjusting their residue oil processing routes and fuel structures; in this process, the partial oxidation gasification technology of deoiled bitumen and petroleum coke has gradually gained market favor. As vanadium, nickel, and other metallic elements in crude oil are gradually enriched into residual oil, petroleum coke, and deoiled bitumen during the refining process, their gasification waste residue contains high levels of heavy metals such as vanadium and nickel (vanadium and nickel content is close to that of vanadium / nickel ore, possessing vanadium and nickel recovery value and leaching toxicity). This gives gasification waste residue the dual attributes of hazardous solid waste and high-value metal (vanadium and nickel) resources. With the promotion of gasification technology for heavy oil-based feedstocks such as deoiled bitumen and petroleum coke, the production and discharge of gasification waste residue will increase year by year. Improper disposal will cause serious environmental problems, making the development of resource utilization technology for gasification waste residue an urgent matter.

[0003] However, gasification waste residue has a high fixed carbon content, low volatile matter content, and poor combustion reactivity, making it difficult to ignite and burn completely, thus posing a challenge for treatment. Summary of the Invention

[0004] The purpose of this disclosure is to address the shortcomings of existing methods in treating gasification waste residue by providing a method for the co-treatment of gasification waste residue and oil sludge.

[0005] The inventors of this disclosure discovered that by co-firing oil sludge residue with gasification waste residue, the iron, alkali metals, alkaline earth metals, and other elements in the oil sludge residue catalyze the combustion reaction of the gasification waste residue, promoting the volatilization and release of the gasification waste residue, increasing the combustion reaction rate and burnout rate, and making the decarbonization treatment of the gasification waste residue more efficient and complete; at the same time, the residual organic matter in the oil sludge residue is completely burned off, achieving complete reduction of oil sludge; thus, this invention was obtained.

[0006] To achieve the above objectives, this disclosure provides a method for the co-treatment of gasification waste residue and oil sludge, wherein the gasification waste residue is the waste residue obtained after preparing syngas from heavy oil-based feedstock, and the method includes:

[0007] S1. The gasification waste residue and oil sludge residue are uniformly mixed to form a first mixture; the oil sludge residue is the residue obtained after oil sludge has undergone dehydration and deoiling treatment.

[0008] S2. The first mixture is subjected to combustion decarbonization.

[0009] Optionally, the method further includes drying and dehydrating the gasification waste residue before uniformly mixing it with the oil sludge residue.

[0010] Optionally, the drying and dehydration conditions are as follows: the drying temperature is 100-120℃, preferably 105-110℃; the drying time is 2-8h, preferably 4-5h.

[0011] Optionally, the moisture content in the dried gasification waste residue is 0-2% by weight, preferably 0-1% by weight.

[0012] Optionally, in step S1, the weight ratio of the gasification waste residue to the oil sludge residue is 100:(0.1-15).

[0013] Preferably, in step S1, the weight ratio of the gasification waste residue to the oil sludge residue is 100:(1-12).

[0014] Optionally, in step S2, the combustion decarburization temperature is 550-650℃, and the time is 1-6 hours; the atmosphere for combustion decarburization is air.

[0015] Preferably, the combustion decarburization temperature is 580-620℃ and the time is 1-4 hours.

[0016] Optionally, the heavy oil-based feedstock includes at least one of residual oil, deoiled bitumen, and petroleum coke.

[0017] Optionally, the method further includes using the high-temperature flue gas generated from combustion decarbonization for the drying and dehydration process.

[0018] Optionally, the method further includes: extracting metallic nickel and / or metallic vanadium from the combustion-decarburized ash.

[0019] Through the above technical solution, the method described in this disclosure has the following beneficial effects: This method co-fires oily sludge residue with gasification waste residue, utilizing elements such as iron, alkali metals, and alkaline earth metals in the oily sludge residue to catalyze the combustion reaction of the gasification waste residue, promoting the volatilization and release of the gasification waste residue, increasing the combustion reaction rate and burnout rate, making the decarbonization treatment of the gasification waste residue more efficient and complete, and facilitating the more economical recovery of vanadium and / or nickel resources from the gasification waste residue; at the same time, it completely burns away the residual organic matter in the oily sludge residue, achieving complete reduction of oily sludge. In addition, this disclosure can also utilize the heat of the high-temperature flue gas emitted from the incinerator to heat the gasification waste residue, thereby removing moisture from the gasification waste residue.

[0020] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Detailed Implementation

[0021] The following provides a detailed description of specific embodiments of this disclosure. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit this disclosure.

[0022] This disclosure provides a method for the co-treatment of gasification waste residue and oil sludge, wherein the gasification waste residue is the waste residue obtained after preparing syngas from heavy oil-based feedstock, and the method includes:

[0023] S1. The gasification waste residue and oil sludge residue are uniformly mixed to form a first mixture; the oil sludge residue is the residue obtained after oil sludge has undergone dehydration and deoiling treatment.

[0024] S2. The first mixture is subjected to combustion decarbonization.

[0025] According to this disclosure, the oil sludge residue is a solid residue after various dehydration and deoiling treatments of oil sludge; the main inorganic elements in the oil sludge residue include at least one or more of iron, alkali metals, and alkaline earth metals; the heavy oil-based raw material includes at least one of residual oil, deoiled asphalt, and petroleum coke; the gasification waste residue is generated during the process in which the heavy petroleum-based gasification raw material undergoes a partial oxidation reaction with the gasifying agent (oxygen, steam) in a gasifier under high temperature and high pressure to generate syngas.

[0026] The method disclosed herein mixes oily sludge residue with gasification waste residue for combustion decarbonization treatment. Elements such as iron, alkali metals, and alkaline earth metals in the oily sludge residue can effectively catalyze the combustion reaction of the gasification waste residue, promote the release of volatile components in the gasification waste residue, and improve the combustion reaction rate and burnout rate, making the decarbonization treatment of the gasification waste residue more efficient and complete. Moreover, the oily sludge residue has poor combustibility after deoiling treatment, and conventional incineration would require a large amount of heat. However, by co-treating it with gasification waste residue, which has a high carbon content, the residual organic matter in the oily sludge residue can be completely burned off without adding other fuels, thus achieving complete reduction of oily sludge.

[0027] Before uniformly mixing the gasification waste residue with the oil sludge residue, the method provided in this disclosure further includes drying and dehydrating the gasification waste residue. As the moisture content decreases, the residual carbon in the gasification waste residue is more easily combusted, achieving a good decarbonization effect. The material obtained after drying and dehydrating the gasification waste residue is uniformly mixed with the oil sludge residue to form a first mixture. The drying and dehydration process removes water introduced during the preparation of syngas from heavy oil-based feedstocks.

[0028] According to this disclosure, the drying and dehydration conditions are not particularly limited, for example, the drying temperature is 100-120℃, preferably 105-110℃; the drying time is 2-8h, preferably 4-5h.

[0029] According to this disclosure, the moisture content in the dried gasification waste residue can be 0-2% by weight, preferably 0-1% by weight.

[0030] According to this disclosure, in step S1, the weight ratio of the gasification waste residue to the oil sludge residue is preferably 100:(0.1-15), more preferably 100:(1-12). Under this preferred condition, combustion decarbonization can be further promoted.

[0031] According to this disclosure, in step S2, the combustion decarburization temperature can be 550-650℃, preferably 580-620℃, and the time can be 1-6 hours, preferably 1-4 hours; the combustion decarburization atmosphere can be air.

[0032] The high-temperature flue gas generated during combustion decarbonization in this disclosure can be sent to a gasification waste residue dryer to remove moisture from the gasification waste residue using the heat of the flue gas. Therefore, preferably, the method described in this disclosure further includes using the high-temperature flue gas generated during combustion decarbonization for the drying and dehydration process.

[0033] According to this disclosure, the treatment of gasification waste residue can be achieved by obtaining ash residue through combustion decarburization. The ash residue obtained from combustion decarburization contains metallic nickel and / or metallic vanadium, and has a high burnout rate, thus greatly reducing the carbon content. Preferably, the method may further include: extracting metallic nickel and / or metallic vanadium from the combustion decarburization ash residue. The extraction of metallic nickel may include acid leaching-ion exchange-alkali nickel precipitation. The extraction of metallic vanadium may include alkaline leaching-ion exchange-ammonium salt vanadium precipitation, etc.

[0034] According to a particularly preferred embodiment of this disclosure, the method comprises: drying and dehydrating the gasification waste residue obtained after preparing syngas from the heavy oil-based raw material at a drying temperature of 105-110℃ for 3-5 hours, resulting in a moisture content of 0-1% by weight for the dried gasification waste residue; then uniformly mixing the dried gasification waste residue with oil sludge residue at a weight ratio of 100:(1-12) to form a first mixture; subjecting the first mixture to combustion decarbonization at 580-620℃ in an air atmosphere for 1-4 hours; the ash residue from the combustion decarbonization can be used to extract metallic nickel and / or metallic vanadium; and the high-temperature flue gas generated during the combustion decarbonization process can be used for drying and dehydrating the gasification waste residue.

[0035] The present disclosure will be further illustrated by the following examples, but the present disclosure is not limited thereto.

[0036] Unless otherwise specified, the raw materials, reagents, instruments and equipment involved in the embodiments of this disclosure can all be obtained by purchase.

[0037] The gasification waste used in the embodiments and comparative examples of this disclosure comes from the de-oiled asphalt gasification hydrogen production unit of a certain refinery. The gasification waste contains 82.4% water before drying. The properties of the gasification waste after drying are shown in Table 1. The oil sludge residue used in the embodiments and comparative examples is the solid residue of the bottom sludge of a crude oil tank area after dehydration and deoiling. Its properties are shown in Table 2.

[0038] Example 1

[0039] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was mixed with oil sludge residue at a mass ratio of 99:1, and then transferred to a muffle furnace at 600℃ under air atmosphere for incineration and decarbonization. After 1 hour, 2 hours, 3 hours, and 4 hours of incineration, the combustible content of the remaining solid ash was 88.02%, 81.83%, 44.71%, and 1.01%, respectively.

[0040] Example 2

[0041] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was mixed with oil sludge residue at a mass ratio of 97:3, and then transferred to a muffle furnace at 600℃ under air atmosphere for incineration and decarbonization. After 1 hour, 2 hours, 3 hours, and 4 hours of incineration, the combustible content of the remaining solid ash was 83.33%, 69.13%, 40.18%, and 0.69%, respectively.

[0042] Example 3

[0043] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was mixed evenly with oil sludge residue at a mass ratio of 95:5, and then transferred to a muffle furnace at 600℃ under air atmosphere for incineration and decarbonization. After 1 hour, 2 hours, and 4 hours of incineration, the combustible content of the remaining solid ash was 81.88%, 68.02%, and 0.22%, respectively.

[0044] Example 4

[0045] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was mixed evenly with oil sludge residue at a mass ratio of 90:10, and then transferred to a muffle furnace at 600℃ for incineration and decarbonization. After 1 hour, 2 hours, 3 hours, and 4 hours of incineration, the combustible content of the remaining solid ash was 75.33%, 57.67%, 23.45%, and 0%, respectively.

[0046] Comparative Example 1

[0047] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was then transferred to a muffle furnace at 500℃ in an air atmosphere for incineration and decarbonization. After 1 hour, 2 hours, 3 hours, 4 hours, and 5 hours of incineration, the combustible content of the remaining solid ash was 89.70%, 85.31%, 74.62%, 56.39%, and 1.34%, respectively.

[0048] Comparative Example 2

[0049] The gasification waste residue was dried in an oven at 105℃ for 4 hours to obtain the dried gasification waste residue (properties shown in Table 2). The dried gasification waste residue was then transferred to a muffle furnace at 600℃ in an air atmosphere for incineration and decarbonization. After 1 hour, 2 hours, 3 hours, and 4 hours of incineration, the combustible content of the remaining solid ash was 88.44%, 81.98%, 49.26%, and 3.21%, respectively.

[0050] Table 1. Basic properties of gasification waste residue after drying

[0051] w(moisture) / % 0.98 w(C) / % 86.33 w(ash content) / % 5.88 w(H) / % 0.77 w(volatile matter) / % 7.04 w(S) / % 3.23 w(fixed carbon) / % 86.10 w(N) / % 0.95 <![CDATA[Gross calorific value / (MJ·kg -1 )]]> 29.50 w(V) / % 2.70 Loss on ignition (600℃) / % 93.89 w(Ni) / % 1.20 w(Fe) / % 0.25

[0052] Table 2. Basic Properties of Oil Sludge Residue

[0053] w(oil) / % 4.40 <![CDATA[w(Na2O) / %]]> 0.943 <![CDATA[w(V2O5) / %]]> 0.163 w(ash content) / % 68.23 w(MgO) / % 1.0 w(MnO) / % 0.789 <![CDATA[Gross calorific value / (MJ·kg -1 )]]> 8.51 <![CDATA[w(Al2O3) / %]]> 3.34 <![CDATA[w(Fe2O3) / %]]> 60.6 <![CDATA[w(SiO2) / %]]> 8.23 w(NiO) / % 0.0574 <![CDATA[w(P2O5) / %]]> 0.149 w(CuO) / % 0.0546 <![CDATA[w(SO3) / %]]> 13.4 w(ZnO) / % 0.543 <![CDATA[w(K2O) / %]]> 0.645 w(SrO) / % 0.158 w(CaO) / % 9.23 w(BaO) / % 0.268 <![CDATA[w(TiO2) / %]]> 0.179

[0054] As can be seen from Examples 1-4 and Comparative Examples 1-2, the method provided in this disclosure utilizes elements such as iron, alkali metals, and alkaline earth metals in the oil sludge residue to catalyze the combustion reaction of the gasification waste residue, promote the volatilization and release of the gasification waste residue, increase the combustion reaction rate and burnout rate, and make the decarbonization treatment of the gasification waste residue more efficient and complete; at the same time, it completely burns away the residual organic matter in the oil sludge residue, achieving complete reduction of oil sludge, which is of great significance for improving resource utilization and environmental protection.

[0055] The preferred embodiments of this disclosure have been described in detail above. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0056] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0057] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A method for co-treating gasification waste residue and oil sludge, wherein the gasification waste residue is the waste residue obtained after preparing syngas from heavy oil-based feedstock, characterized in that, The method includes: S1. The gasification waste residue and the oil sludge residue are mixed evenly to form a first mixture; the oil sludge residue is the residue obtained after the oil sludge has been dehydrated and deoiled, including iron, alkali metals and alkaline earth metals; in step S1, the weight ratio of the gasification waste residue to the oil sludge residue is 100:(0.1-15). S2. The first mixture is subjected to combustion decarbonization; wherein the iron, alkali metal, and alkaline earth metal elements are used to catalyze the combustion decarbonization reaction of the gasification waste residue in the first mixture. The combustion decarburization temperature is 550-650℃, and the time is 1-6 hours; The method further includes drying and dehydrating the gasification waste residue before uniformly mixing it with the oil sludge residue; The high-temperature flue gas generated from the combustion decarbonization is used for the drying and dehydration process.

2. The method according to claim 1, wherein, The drying and dehydration conditions are as follows: drying temperature is 100-120℃, and drying time is 2-8h.

3. The method according to claim 2, wherein, The drying and dehydration conditions are as follows: drying temperature is 105-110℃, and drying time is 4-5 hours.

4. The method according to claim 3, wherein, The moisture content of the dried gasification waste residue is 0-2% by weight.

5. The method according to claim 1, wherein, In step S1, the weight ratio of the gasification waste residue to the oil sludge residue is 100:(1-12).

6. The method according to claim 1, wherein, In step S2, the atmosphere for combustion decarburization is air; the temperature for combustion decarburization is 580-620℃, and the time is 1-4 hours.

7. The method according to claim 1, wherein, The heavy oil-based feedstock includes at least one of residual oil, deoiled bitumen, and petroleum coke.

8. The method according to claim 1, wherein, The method also includes the operation of extracting metallic nickel and / or metallic vanadium from the ash residue after combustion decarburization.