Process and system for pulping by mixing oil-water phase waste liquid and carbon raw material

Abstract

The invention discloses an oil-water phase waste liquid and carbon raw material mixed pulping process and system.The oil-water phase waste liquid and carbon raw material mixed pulping process comprises the steps that firstly, oil phase waste liquid is pumped into a homogenizing tank, and first circulation is established on the homogenizing tank; a static mixer is arranged in the first cycle, water-phase waste liquid and an additive are supplemented into the first cycle through the static mixer, after the water-phase waste liquid and the additive are completely added into a homogenizing tank through the static mixer, oil-water mixed liquid is obtained through first cycle homogenization, and the volume ratio of the oil-phase waste liquid to the water-phase waste liquid is gt; 0.9, the content of the additive is 0.1%-1.5%; mixing and pulping the carbon black and the oil-water mixed solution to obtain slurry with the mass concentration of the carbon black being 5-15%; according to the invention, waste water, waste oil and carbon black can be used for pulping at the same time, and the prepared slurry has the advantages of stable gasification, high waste liquid treatment efficiency, no secondary pollution and the like when applied to a gasification furnace.

Description

Technical Field

[0001] The invention relates to the technical field of resource utilization of oily waste liquid, and in particular to a process and system for mixing oily waste liquid with carbon raw materials to make pulp. Background Art

[0002] Wastewater treatment is a crucial process in the fields of chemical equipment and machinery, environmental engineering, and chemical processes. In particular, in industries such as petrochemicals and coal chemical processing, large quantities of oily and aqueous wastewater are generated. These wastewaters contain significant amounts of organic pollutants, which, if left untreated, can cause serious environmental pollution. Existing technologies typically utilize physical and chemical methods, such as extraction, precipitation, and adsorption, to treat organic pollutants in wastewater. However, these methods often suffer from low treatment efficiency, high costs, and the tendency to generate secondary pollution.

[0003] Currently, there are also disclosed resource utilization methods for mixing oily and water waste liquid with other carbon-containing materials, pulping them, and then feeding them into a gasifier to produce synthesis gas. The resulting synthesis gas contains relatively high levels of hydrogen and CO. However, the existing pulping processes all use wastewater or waste oil to mix carbon black particles separately. If wastewater and waste oil are used together with carbon black to produce pulp, stratification and carbon black clumping are likely to occur. When these are fed into the gasifier, the gasifier may not operate stably. Therefore, the existing technology is unable to simultaneously process both oily and water-phase waste liquids, and the resulting slurry is not stable. Summary of the Invention

[0004] Therefore, the technical problem to be solved by the present invention is to overcome the problem that the pulping process in the prior art cannot use wastewater and waste oil and carbon black for pulping at the same time, thereby providing a process and system for pulping mixed oil-water phase waste liquid and carbon raw materials to solve the above problem.

[0005] A process for mixing oil-water phase waste liquid with carbon raw material to prepare pulp, comprising:

[0006] First, the oil phase waste liquid is pumped into the homogenizing tank and the first circulation is established on the homogenizing tank;

[0007] A static mixer is provided in the first cycle, and the aqueous phase waste liquid and the additive are fed into the first cycle through the static mixer. After the aqueous phase waste liquid and the additive are completely added to the homogenizing tank through the static mixer, an oil-water mixture is obtained by homogenizing through the first cycle, wherein the volume ratio of the oil phase waste liquid to the aqueous phase waste liquid is greater than 0.9, and the content of the additive is 0.1% to 1.5%; for example, the volume ratio of the oil phase waste liquid to the aqueous phase waste liquid is 0.9, 1, 1.2, 1.5, 1.8, 2, 3, 5, 8, etc., and the content of the additive is 0.1%, 0.2%, 0.3%, 0.4%, 0.5%, 0.6%, 0.7%, 0.8%, 0.9%, 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, etc.;

[0008] Carbon black and an oil-water mixture are slurried to obtain a slurry with a carbon black mass concentration of 5% to 15%; for example, the mass concentration of carbon black in the slurry is 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15%, etc.

[0009] In a preferred embodiment, the additive comprises at least 0.1% to 0.5% of a dispersant, and preferably, further comprises 0.1% to 1.0% of a stabilizer. For example, the mass concentration of the dispersant in the slurry is 0.1%, 0.2%, 0.3%, 0.4%, 0.5%, etc., and the mass concentration of the stabilizer in the slurry is 0.1%, 0.2%, 0.3%, 0.4%, 0.5%, 0.6%, 0.7%, 0.8%, 0.9%, 1.0%, etc.

[0010] Furthermore, the dispersant includes but is not limited to lignin sulfonate dispersants, humic acid dispersants, and polycarboxylic acid dispersants;

[0011] And / or, the stabilizer includes but is not limited to organic polymer stabilizers, natural polymer stabilizers, and surfactants.

[0012] In a preferred embodiment, the mass concentration of carbon black in the slurry is 6% to 8%.

[0013] In a preferred embodiment, the temperature of the oil-water mixture is 20-90°C; for example, the temperature of the oil-water mixture is 20°C, 25°C, 30°C, 35°C, 40°C, 45°C, 50°C, 55°C, 60°C, 65°C, 70°C, 75°C, 80°C, 85°C, 90°C, etc.

[0014] In a preferred embodiment, the operating temperature of the static mixer is 40-50°C, and the operating pressure is 1-2.5 MPa; for example, the operating temperature is 40°C, 42°C, 44°C, 46°C, 48°C, 50°C, etc., and the operating pressure is 1 MPa, 1.5 MPa, 2.0 MPa, 2.5 MPa, etc.

[0015] A slurry for a gasifier is prepared by adopting the above-mentioned process of mixing an oil-water phase waste liquid with a carbon raw material to prepare a slurry.

[0016] An application of a slurry for gasification in a gasifier to generate synthesis gas, wherein the slurry is prepared by the above-mentioned process of mixing an oil-water phase waste liquid with a carbon raw material;

[0017] The process conditions for gasification in the gasifier are as follows: the temperature is controlled at 1000-1300°C, preferably 1100-1200°C; the pressure is controlled at 1.0-2.5 MPa, preferably 1.1-1.6 MPa; the gas flow rate is controlled at 2-4 m / s, preferably 2.5-3.5 m / s; the oxygen-fuel ratio is controlled at 0.5-0.9, preferably 0.6-0.7; and the oxygen-liquid ratio is controlled at 0.3-0.6, preferably 0.4-0.5.

[0018] In the above-mentioned gasification process conditions, the temperature can be controlled to 1000°C, 1050°C, 1100°C, 1150°C, 1200°C, 1250°C, 1300°C, etc., the pressure can be controlled to 1MPa, 1.5MPa, 2.0MPa, 2.5MPa, etc., the gas flow rate can be controlled to 2m / s, 2.5m / s, 3m / s, 3.5m / s, 4m / s, etc., the oxygen-fuel ratio can be controlled to 0.5, 0.6, 0.7, 0.8, 0.9, etc., and the oxygen-liquid ratio can be controlled to 0.3, 0.4, 0.5, 0.6, etc.

[0019] A system for mixing oil-water phase waste liquid with carbon raw material to make pulp, comprising:

[0020] Homogenizing tank, including oily waste liquid inlet, circulating liquid inlet and outlet;

[0021] A static mixer is connected to the outlet of the homogenizing tank;

[0022] The circulation pipeline has two ends connected to the outlet of the static mixer and the circulating liquid inlet of the homogenizing tank respectively, forming a first circulation with the static mixer and the homogenizing tank;

[0023] The oily waste liquid storage tank is connected to the oily waste liquid inlet of the homogenizing tank;

[0024] Aqueous waste liquid storage tank connected to the inlet of the static mixer;

[0025] The pulping unit is connected to the outlet of the static mixer.

[0026] A homogenizing pump is also provided on the circulation pipeline;

[0027] A cooler is also provided on the circulation pipeline at a position adjacent to the circulating liquid inlet of the homogenizing tank;

[0028] An oily waste liquid delivery pump is provided at the outlet of the oily waste liquid storage tank, and an oily waste liquid return pipeline connected to the oily waste liquid storage tank is connected to the outlet of the oily waste liquid delivery pump;

[0029] An aqueous waste liquid delivery pump is provided at the outlet of the aqueous waste liquid storage tank, and an aqueous waste liquid return pipeline connected to the aqueous waste liquid storage tank is connected to the outlet of the aqueous waste liquid delivery pump;

[0030] The system further comprises an additive storage tank, the outlet of which is in communication with the inlet of the static mixer.

[0031] The carbon black in the present invention can be acetylene black, that is, carbon black produced as a by-product in the acetylene production process, thereby achieving the purpose of full waste utilization.

[0032] The technical solution of the present invention has the following advantages:

[0033] The process for mixing oil-water phase waste liquid with carbon raw material for pulping provided by the present invention can simultaneously use wastewater, waste oil and carbon black for pulping, has no requirements for the particle size of the carbon source material, and the preparation process has the advantages of high waste liquid treatment efficiency and no secondary pollution. The prepared slurry has high stability. When the prepared slurry is applied to a gasifier, it has gasification stability, thereby increasing the yield of effective gas in the synthesis gas. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0035] Figure 1 This is a structural diagram of a system for mixing oil-water phase waste liquid with carbon raw material for pulping in Example 1 of the present invention;

[0036] Reference numerals:

[0037] 1-Oily waste liquid storage tank, 2-Oily waste liquid delivery pump, 3-Homogenizing tank, 4-Homogeneous material delivery pump, 5-Static mixer, 6-Homogenizing pump, 7-Cooler, 8-Aqueous waste liquid storage tank, 9-Aqueous waste liquid delivery pump, 10-Pulping unit. DETAILED DESCRIPTION

[0038] The following examples are provided for a better understanding of the present invention and are not intended to limit the best mode of implementation. They do not limit the content and scope of protection of the present invention. Any product identical or similar to the present invention obtained by anyone under the guidance of the present invention or by combining the features of the present invention with other prior arts shall fall within the scope of protection of the present invention.

[0039] If no specific experimental steps or conditions are specified in the examples, the conventional experimental steps or conditions described in the literature in this field can be used. If the manufacturer of the reagents or instruments is not specified, they are all commercially available conventional reagents.

[0040] Example 1

[0041] A system for mixing oil-water phase waste liquid with carbon raw material to make pulp, such as Figure 1 As shown, it includes a homogenizing tank 3, a circulation pipeline, an oily waste liquid storage tank 1, an aqueous waste liquid storage tank 8, and a pulping unit 10. The homogenizing tank 3 includes an oily waste liquid inlet, a circulating liquid inlet, and an outlet; the static mixer 5 is connected to the outlet of the homogenizing tank 3; the two ends of the circulation pipeline are connected to the outlet of the static mixer 5 and the circulating liquid inlet of the homogenizing tank 3, respectively, and the circulation pipeline, the static mixer 5, and the homogenizing tank 3 form a first loop; the oily waste liquid storage tank 1 is connected to the oily waste liquid inlet of the homogenizing tank 3; the aqueous waste liquid storage tank 8 is connected to the inlet of the static mixer 5; and the pulping unit 10 is connected to the outlet of the static mixer 5. In the system of the present invention, a homogenizing pump 6 is further provided on the circulation pipeline; a cooler 7 is further provided on the circulation pipeline at a position adjacent to the circulating liquid inlet of the homogenizing tank 3; an oily waste liquid delivery pump 2 is provided at the outlet of the oily waste liquid storage tank 1, and the outlet of the oily waste liquid delivery pump 2 is connected to an oily waste liquid reflux pipeline connected to the oily waste liquid storage tank 1; an aqueous waste liquid delivery pump 9 is provided at the outlet of the aqueous waste liquid storage tank 8, and the outlet of the aqueous waste liquid delivery pump 9 is connected to an aqueous waste liquid reflux pipeline connected to the aqueous waste liquid storage tank 8; a homogenizing material delivery pump 4 is further provided between the homogenizing tank 3 and the static mixer 5; the system also includes an additive storage tank, whose outlet is connected to the inlet of the static mixer 5.

[0042] The process of mixing and pulping using the above-mentioned system for mixing oil-water phase waste liquid with carbon raw material in the present invention is as follows:

[0043] Step 1: The oily phase waste liquid and the aqueous phase waste liquid are respectively transported to separate storage tanks, and the oily waste liquid is pumped from the oily waste liquid storage tank 1 into the homogenizing tank 3 via the oily waste liquid delivery pump 2. After a certain liquid level is established, the oily waste liquid feed is closed; in this embodiment, the liquid level of the oily waste liquid is 48% of the total storage liquid level of the homogenizing tank 3;

[0044] Step 2: Start the homogenizing material delivery pump 4 and the homogenizing pump 6 to allow the waste liquid to pass through the material delivery pump 4, the static mixer 5, the homogenizing pump 6, and the cooler 7 provided on the circulation pipeline at the outlet of the homogenizing tank 3 to cool down and then return to the homogenizing tank 3 to form the first circulation;

[0045] Step 3: Turn on the aqueous waste liquid delivery pump 9, and the aqueous waste liquid flows back from the aqueous waste liquid storage tank 8 through the reflux line to the aqueous waste liquid storage tank 8. After the flow rate is established and stabilized, it is merged into the static mixer 5. At the same time, the additive is pumped into the static mixer 5 through the flow meter according to a certain proportion, and then enters the homogenizing tank 3 through the homogenizing pump 6 cooler 7. The liquid level in the homogenizing tank 3 rises slowly;

[0046] Step 4: Control the ratio of oily waste liquid and aqueous waste liquid to a certain value. When the liquid level of the homogenizing tank 3 reaches 80%, stop feeding the aqueous waste liquid and the additive. In this embodiment, the volume ratio of the oily waste liquid and the aqueous waste liquid is 48% / 32%=1.5. After the homogenizing tank 3 reaches 80% of the liquid level, the first cycle homogenization of the homogenizing tank 3 is started. The time of the first cycle homogenization is 5 minutes. In this embodiment, the additives include 0.3% of the total mass of the oily waste liquid and the aqueous waste liquid. A lignin sulfonate dispersant: sodium lignin sulfonate and 0.3% of an organic polymer stabilizer: sodium polystyrene sulfonate (manufacturer: Aksu).

[0047] Step 5: After homogenization is completed, the mixed oil-water mixture is transported to the pulping unit through a pipeline, and pulped with carbon black to obtain a slurry with a carbon black mass content of 8%; the slurry is then sent to the gasifier through a feed pump for gasification.

[0048] The process of gasification using the above-mentioned slurry in the present invention is as follows: in the gasifier, operating conditions such as temperature, pressure, gas flow rate, etc. are controlled to improve the efficiency and stability of waste liquid treatment; specifically, the gasification temperature is selected to be 1100°C, the pressure is 1.5MPa, the flow rate is 3m / s, the oxygen-fuel ratio is controlled to be 0.6, and the oxygen-liquid ratio is controlled to be 0.35.

[0049] The product (synthesis gas) after the gasification furnace treatment is output through the pipeline, completing the waste liquid treatment process. The present invention regularly maintains and overhauls the system to ensure the normal operation of the system and the stability of the waste liquid treatment.

[0050] Example 2

[0051] The difference from Example 1 is that in this embodiment, the homogenizing tank 3 establishes a 40% liquid level of oily waste liquid, and the aqueous waste liquid is then pumped into the liquid level of 40%. The volume ratio of the oily phase waste liquid to the aqueous phase waste liquid is approximately 1, and the other conditions are the same as in Example 1.

[0052] Example 3

[0053] The difference from Example 1 is that the additive in this example is only 0.6% sodium lignin sulfonate, and the other conditions are the same as those in Example 1.

[0054] Example 4

[0055] The difference from Example 1 is that the additives in this example are 0.1% of a humic acid dispersant: sodium humate and 0.3% of an organic polymer stabilizer: sodium carboxymethyl cellulose (Xinghua brand, XH-666). The other conditions are the same as in Example 1.

[0056] Example 5

[0057] The difference from Example 1 is that the additives in this embodiment are 0.5% of a polycarboxylic acid dispersant: a polycarboxylic acid water reducer (Bohao, BH4) and 1% of a surfactant: lauryl alcohol polyoxyethylene ether (Haishihua, AEO-5), and the other conditions are the same as in Example 1.

[0058] Example 6

[0059] The difference from Example 1 is that the mass content of carbon black in the slurry of this example is 6%, and the other conditions are the same as those in Example 1.

[0060] Example 7

[0061] The difference from Example 1 is that the mass content of carbon black in the slurry of this example is 13%, and the other conditions are the same as those in Example 1.

[0062] Example 8

[0063] The difference from Example 1 is that in the gasification step of this embodiment, the oxygen-fuel ratio is controlled to be 0.7 and the oxygen-liquid ratio is controlled to be 0.5, and the other conditions are the same as those in Example 1.

[0064] Example 9

[0065] The difference from Example 1 is that in the gasification step of this embodiment, the oxygen-fuel ratio is controlled to be 0.4 and the oxygen-liquid ratio is controlled to be 0.2, and the other conditions are the same as those in Example 1.

[0066] Example 10

[0067] The difference from Example 1 is that the time for the first cycle homogenization in this embodiment is 20 minutes, and the other conditions are the same as those in Example 1.

[0068] Comparative Example 1

[0069] The difference from Example 1 is that in this comparative example, the homogenizing tank 3 establishes a 32% liquid level of oily waste liquid, and the aqueous waste liquid is then pumped into the homogenizing tank 3 to a 48% liquid level. The volume ratio of the oily phase waste liquid to the aqueous phase waste liquid is approximately 0.67, and the other conditions are the same as in Example 1.

[0070] Comparative Example 2

[0071] The difference from Example 1 is that there is no additive in this comparative example, and the other conditions are the same as those in Example 1.

[0072] Comparative Example 3

[0073] The difference from Example 1 is that in this comparative example, the outlet of the aqueous waste liquid storage tank 8 is directly connected to the oily waste liquid inlet of the homogenizing tank 3. That is, without preliminary mixing in a static mixer, the aqueous waste liquid and the oily waste liquid are directly transported to the homogenizing tank 3 for direct mixing. After the aqueous waste liquid and the oily waste liquid are completely added to the homogenizing tank 3, they are homogenized and mixed for 5 minutes to obtain an oil-water mixture. The remaining conditions in this comparative example are the same as those in Example 1.

[0074] Experimental example

[0075] The slurries of the examples and comparative examples were tested for the proportion of slurry particles (1-4 mm) and stability, and the composition of the syngas after gasification was tested. The test results are shown in Table 1 below.

[0076] The percentage of slurry particles (1-4 mm and >4 mm) is determined by sieving and weighing: Weigh 100 g of slurry and pass it through a 4 mm sieve and then a 1 mm sieve. Rinse the carbon black particles on the sieves with water for 3 minutes and then dry them in a 105°C oven for 2 hours. Weigh the carbon black particles m1 and m2 with a particle size >4 mm and between 1 and 4 mm. The percentage of carbon black particles with a particle size >4 mm = m1 / 100; the percentage of carbon black particles with a particle size between 1 and 4 mm = m2 / 100.

[0077] The stability test method is: GB-T 18856.5-2008 Test Methods for Coal-Water Slurries Part 5: Determination of Stability. This patent mainly analyzes static stability. When the stability value is less than 0.5%, it is indicated by Y (Excellent); when the stability value is between 0.5% and 2%, it is indicated by Z (Fair); when the stability value is greater than 2%, it is indicated by X (Poor).

[0078] The detection method of synthesis gas is: gas chromatograph (equipment model: Agilent 8860).

[0079] Table 1

[0080]

[0081]

[0082] From the data in Table 1 above, we can see that the factors affecting the pulping effect include the oil-water mixing ratio, the type and dosage of additives used, the mass content of carbon black, and the homogenization method and time.

[0083] Comparison of the data from Examples 1 and 2 and Comparative Example 1 shows that the higher the ratio of oily waste liquid to aqueous waste liquid, the better the dispersibility and stability of the resulting finished slurry. When the ratio of oily waste liquid to aqueous waste liquid is less than 0.9, no qualified slurry can be obtained. This is presumably because the surface of the carbon black particles is hydrophobic. When the oil-water ratio is less than 0.9, the homogenization results in a primarily oil-in-water emulsion. In this case, the carbon black particles are adsorbed into the oil droplets in the water, forming water-in-carbon black, which prevents slurrying.

[0084] Comparison of the five data sets in Examples 1, 3, 4, and 5, as well as Comparative Example 2, shows that qualified slurry cannot be obtained without the use of additives. The additives must include at least a dispersant. The dispersant is an amphiphilic substance, with one lipophilic end adsorbed on the carbon black surface and the other hydrophilic end in contact with water in the wastewater, forming a more stable system while preventing carbon black particles from agglomerating and increasing their dispersibility. Different additive compositions and dosages have varying effects on slurry formation. Dispersants in the present invention include, but are not limited to, lignin sulfonate dispersants, humic acid dispersants, and polycarboxylic acid dispersants, with lignin sulfonate being preferred. Stabilizers include, but are not limited to, organic polymer stabilizers, natural polymer stabilizers, and surfactants, with sodium polystyrene sulfonate being preferred. The dispersant dosage is 0.1% to 0.5%, preferably 0.2% to 0.4%, and the stabilizer dosage is 0.1% to 1.0%, preferably 0.2% to 0.5%. The combination of dispersants and stabilizers is not limited to that described in the above examples.

[0085] From the comparison of the data of Examples 1, 6 and 7, it can be seen that different amounts of carbon black added have a greater impact on the dispersibility and stability of the slurry. As the carbon black concentration increases, the carbon black dispersibility and stability become worse, and at the same time, the effective gas of the produced synthesis gas becomes lower. The carbon black mass concentration is 5% to 15%, and the preferred carbon black mass concentration is 6% to 8%.

[0086] Based on the data from Examples 1, 8, and 9, for the same slurry, different oxygen-fuel ratios and oxygen-liquid ratios produce significantly different syngas components. The higher the oxygen content, the more complete the combustion, the higher the CO2 content in the syngas, and the lower the CO content. For this type of slurry, the hydrogen concentration produced is also higher. Therefore, the oxygen-fuel ratio and oxygen-liquid ratio can be adjusted accordingly based on the intended use of the syngas. In the present invention, the oxygen-fuel ratio is controlled at 0.5 to 0.9, preferably 0.6 to 0.7; the oxygen-liquid ratio is controlled at 0.3 to 0.6, preferably 0.4 to 0.5; at this point, the effective gas (CO + H2) in the syngas can reach over 80%, and typically over 85%.

[0087] Comparison of the data from Examples 1 and 10 and Comparative Example 3 shows that different homogenization methods significantly affect the slurry properties of carbon black. In Comparative Example 3, water was directly introduced into homogenization tank 3 for mixing. However, due to water-oil phase separation, the water phase entering the tank remained in the lower layer. At this point, the circulating homogenized medium would become the water phase, failing to achieve the goal of homogenizing and emulsifying the water and oil together, resulting in subsequent slurrying that could not meet usage requirements. In contrast, in Example 1, water was directly introduced into the static mixer, which allowed for direct emulsification of the oil-water material to produce an emulsion. Furthermore, a longer homogenization time significantly improved the subsequent slurrying process.

[0088] Obviously, the above embodiments are merely examples for clarity of explanation and are not intended to limit the implementation methods. Those skilled in the art will readily appreciate that other variations or modifications based on the above descriptions are possible. It is not necessary and impossible to enumerate all implementation methods here. Obvious variations or modifications arising therefrom remain within the scope of protection of the present invention.

Claims

1. A process for mixing oil-water phase waste liquid with carbon raw material to make pulp, characterized in that: include: First, the oil phase waste liquid is pumped into the homogenizing tank and the first circulation is established on the homogenizing tank; A static mixer is provided in the first cycle, and the aqueous phase waste liquid and the additive are fed into the first cycle through the static mixer. After the aqueous phase waste liquid and the additive are completely added to the homogenization tank through the static mixer, an oil-water mixture is obtained by homogenization through the first cycle, wherein the volume ratio of the oil phase waste liquid to the aqueous phase waste liquid is greater than 0.9, and the content of the additive is 0.1% to 1.5%; The carbon black and the oil-water mixture are pulped to obtain a slurry with a carbon black mass concentration of 5% to 15%.

2. The process according to claim 1, characterized in that The additives include at least 0.1% to 1.5% of a dispersant, and preferably include 0.1% to 0.5% of a dispersant and 0.1% to 1.0% of a stabilizer.

3. The process according to claim 2, characterized in that The dispersant includes but is not limited to lignin sulfonate dispersants, humic acid dispersants, and polycarboxylic acid dispersants; And / or, the stabilizer includes but is not limited to organic polymer stabilizers, natural polymer stabilizers, and surfactants.

4. The process according to any one of claims 1 to 3, characterized in that The mass concentration of carbon black in the slurry is 6% to 8%.

5. The process according to any one of claims 1 to 4, characterized in that The temperature of the oil-water mixture is 20 to 90°C; The time for the first homogenization cycle is 5 to 20 minutes.

6. The process according to any one of claims 1 to 4, characterized in that The operating temperature of the static mixer is 40-50° C., and the operating pressure is 1-2.5 MPa.

7. A slurry for a gasifier, characterized in that: The slurry is prepared by the process of mixing an oil-water phase waste liquid with a carbon raw material as described in any one of claims 1 to 6.

8. An application of slurry in a gasifier to generate synthesis gas by gasification, characterized in that: The slurry is a slurry prepared by the process of mixing an oil-water phase waste liquid with a carbon raw material to make a slurry according to any one of claims 1 to 6; The process conditions for gasification in the gasifier are: the temperature is controlled at 1000-1300°C, preferably 1100-1200°C; and / or the pressure is controlled at 1.0-2.5 MPa, preferably 1.1-1.6 MPa; and / or the gas flow rate is controlled at 2-4 m / s, preferably 2.5-3.5 m / s; and / or the oxygen-fuel ratio is controlled at 0.5-0.9, preferably 0.6-0.7; and / or the oxygen-liquid ratio is controlled at 0.3-0.6, preferably 0.4-0.

5.

9. A system for mixing oil-water phase waste liquid with carbon raw material to make pulp, characterized in that: include: A homogenizing tank (3) including an oily waste liquid inlet, a circulating liquid inlet, and an outlet; A static mixer (5) is connected to the outlet of the homogenizing tank (3); The circulation pipeline has two ends connected to the outlet of the static mixer (5) and the circulating liquid inlet of the homogenizing tank (3), respectively, forming a first circulation with the static mixer (5) and the homogenizing tank (3); The oily waste liquid storage tank (1) is connected to the oily waste liquid inlet of the homogenizing tank (3); an aqueous waste liquid storage tank (8) connected to the inlet of the static mixer (5); The pulping unit (10) is connected to the outlet of the static mixer (5).

10. The system according to claim 9, characterized in that The circulation pipeline is also provided with a homogenizing pump (6); A cooler (7) is also provided on the circulation pipeline at a position adjacent to the circulation liquid inlet of the homogenizing tank (3); An oily waste liquid delivery pump (2) is provided at the outlet of the oily waste liquid storage tank (1), and an oily waste liquid return pipeline in communication with the oily waste liquid storage tank (1) is connected to the outlet of the oily waste liquid delivery pump (2); An aqueous waste liquid delivery pump (9) is provided at the outlet of the aqueous waste liquid storage tank (8), and an aqueous waste liquid return pipeline in communication with the aqueous waste liquid storage tank (8) is connected to the outlet of the aqueous waste liquid delivery pump (9); A homogenized material delivery pump (4) is also provided between the homogenizing tank (3) and the static mixer (5); The system further comprises an additive storage tank, the outlet of which is connected to the inlet of the static mixer (5).

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