Coupling gasification feeding device and method

Abstract

The invention provides a coupling gasification feeding device and method. The problems that a traditional feeding method is high in cost and tedious in configuration, the raw material concentration is prone to fluctuation, and a feeding system is poor in stability are solved. The coupling gasification feeding device comprises a gasification furnace; the burners are distributed at the inlet of the gasification furnace, and each burner comprises a plurality of channels; the channels comprise a slurry channel, an oil product channel and an oxygen channel; the slurry preparation and conveying system is used for preparing slurry and conveying the slurry to the slurry channel; the oil product storage and feeding system is used for storing oil products and conveying the oil products to the oil product channel; the oxygen supply system is used for providing oxygen and conveying the oxygen to the oxygen channel; and the channel control system is used for selecting the slurry channel and the oil product channel from the plurality of channels according to the feed quantity ratio of the oil product and the slurry.

Description

Technical Field

[0001] The invention relates to the technical field of coal chemical industry, and in particular to a coupled gasification feeding device and method. Background Art

[0002] With the increasing environmental protection requirements in various places and the gradual expansion of the ban on high-sulfur petroleum coke leaving the factory, delayed coking is no longer the preferred option for heavy oil processing technology. In recent years, oil refining technology has been innovated and developed. Residue oil solvent deasphalting and residue oil hydrogenation technology have received more and more attention due to their many advantages. However, both residue oil processing processes will produce a certain amount of inferior residue oil. Solving the treatment of this part of inferior residue oil has become the first issue to be considered in the promotion of the two technologies. In addition, the application of hydrogenation technology also needs to solve the problem of hydrogen sources. The main sources of hydrogen in refineries are hydrogen produced as a by-product of catalytic reforming (about 20%) and hydrogen produced as a by-product of various dry gas separations (about 7%). The remaining hydrogen needs to be provided by hydrogen production equipment. With the increasing maturity of coal gasification technology, coal gasification processes that use coal as raw material to provide hydrogen for refineries are becoming more and more widely used. In view of the processing of inferior heavy oil, domestic researchers have carried out a feasibility study on the co-gasification of coal and heavy oil, and verified the feasibility of co-gasification of the two raw materials from a theoretical perspective.

[0003] In the traditional process, oil products and high-carbon slurry are usually made into a special slurry system as a raw material to enter the burner for reaction. This method only needs to configure a feeding system, and the adjustment of the oxygen-carbon ratio is consistent with the gasification process of the same raw material. The control system is relatively simple. However, in order to prepare the mixed slurry system, it is often necessary to select a special compound additive, which is costly and cumbersome to configure, and the raw material concentration is prone to fluctuations. In addition, in order to reduce the viscosity of the mixed slurry, prevent pipeline blockage, and ensure the normal feeding of raw materials, the temperature of the mixed slurry needs to be increased, which can easily cause the coal mill, high-pressure slurry feed pump, etc. to jump due to high temperature, and the system stability is poor. Summary of the invention

[0004] In view of this, an embodiment of the present invention provides a coupled gasification feeding device and method, which solves the problems of high cost and complicated configuration of traditional feeding methods, easy fluctuation of raw material concentration and poor stability of the feeding system.

[0005] In a first aspect, a coupled gasification feeding device provided by an embodiment of the present invention comprises:

[0006] Gasifier;

[0007] A burner is disposed at the inlet of the gasifier, and the burner includes a plurality of channels; the channels include a slurry channel, an oil channel and an oxygen channel;

[0008] A slurry preparation and delivery system, used for preparing slurry and delivering the slurry to a slurry channel;

[0009] Oil storage and feeding system, used to store oil and transport oil to oil channels;

[0010] an oxygen supply system for supplying oxygen and delivering the oxygen to the oxygen passage;

[0011] The channel control system is used to select the slurry channel and the oil channel from the multiple channels according to the feed ratio of the oil product and the slurry.

[0012] In one embodiment, the channel includes a first channel and a second channel; the channel control system is configured to select the first channel as the oil channel and the second channel as the slurry channel when the mass ratio of the oil product to the slurry is between 0.02 and 1; when the mass ratio of the oil product to the slurry is greater than 1, the second channel is selected as the oil channel and the first channel is selected as the slurry channel.

[0013] In one embodiment, the oxygen channel includes a central oxygen channel and an annular oxygen channel; the central oxygen channel is arranged on one side of the second channel; the annular oxygen channel is arranged on the side of the second channel away from the central oxygen channel, and the first channel is arranged on the side of the annular oxygen channel away from the second channel; wherein the central oxygen channel is arranged on the inner side of the burner.

[0014] In one embodiment, when the mass ratio of the oil product to the slurry is greater than 0.4, the channel further includes a protection channel disposed between the oil product channel and the oxygen channel.

[0015] In one embodiment, it further includes: an oxygen-carbon ratio control system for adjusting the input ratio of oxygen.

[0016] In one embodiment, a cooling system is further included, which is arranged on the burner and is used to cool the burner for protection.

[0017] In one embodiment, a high-pressure purge system is further included, which is arranged at the channel of the burner and is used to purge and flush the channel.

[0018] In a second aspect, an embodiment of the present invention provides a coupled gasification feeding method, comprising:

[0019] According to the feed ratio of oil product and slurry, a slurry channel and an oil product channel are selected from multiple channels;

[0020] The slurry is transported to the slurry channel, the oil product is transported to the oil product channel, and the oxygen is transported to the oxygen channel.

[0021] In one embodiment, the method further includes: adjusting the input ratio of oxygen.

[0022] In one embodiment, adjusting the oxygen input ratio comprises:

[0023] Based on the first raw material feed amount, the second raw material feed amount and the reaction temperature, the total effective gas production and the total oxygen consumption under the oil-coal coupled gasification are obtained;

[0024] The reaction temperature and the feed amount of the second raw material are fixed, the effective gas production and oxygen consumption of the second raw material reaction are determined, and the effective gas production and oxygen consumption of the first raw material are obtained based on the total effective gas production and total oxygen consumption, the effective gas production and oxygen consumption of the second raw material reaction;

[0025] Determine the unit effective gas production and unit oxygen consumption of the first raw material and the second raw material based on the first raw material feed amount, the second raw material feed amount, the first raw material effective gas production and oxygen consumption, and the second raw material effective gas production and oxygen consumption;

[0026] Under a preset gas production load, based on the total effective gas production, determining a main raw material and a secondary raw material that affect the total effective gas production from the first raw material and the second raw material;

[0027] The flow rate of the main raw material is fixed, and the flow rate of the secondary raw material is adjusted to a first target flow rate value. During the adjustment process, based on the unit oxygen consumption of the main raw material and the unit oxygen consumption of the secondary raw material, the oxygen consumption of the secondary raw material flow rate and the oxygen consumption of the main raw material are obtained;

[0028] obtaining a first total oxygen demand based on the oxygen consumption of the secondary raw material and the oxygen consumption of the primary raw material;

[0029] After the flow rate of the secondary raw material is adjusted to the first target flow rate value, the flow rate of the secondary raw material is fixed, and under a preset gas production load, a second target flow rate value of the main raw material is obtained based on the total effective gas production, the adjusted flow rate of the secondary raw material, and the unit effective gas production of the secondary raw material, and the flow rate of the main raw material is adjusted to the second target flow rate value;

[0030] During the adjustment process, the oxygen consumption corresponding to the main raw material and the oxygen consumption corresponding to the secondary raw material under the preset gas production load are obtained from the unit oxygen consumption of the main flow and the unit oxygen consumption of the secondary raw material;

[0031] Obtaining a second total oxygen demand based on the oxygen consumption of the secondary raw material flow and the oxygen consumption of the primary raw material;

[0032] The input ratio of oxygen is adjusted based on the first total oxygen demand and the second total oxygen demand.

[0033] In one embodiment, the method comprises: when the mass ratio of the oil product to the slurry is between 0.02 and 1, the first raw material is the oil product and the second raw material is the slurry;

[0034] When the mass ratio of the oil product to the slurry is greater than 1, the first raw material is the slurry, and the second raw material is the oil product.

[0035] In one embodiment, the method comprises: when the mass ratio of the oil product to the slurry is between 0.02 and 0.4, the oil product is the secondary raw material and the slurry is the primary raw material;

[0036] When the mass ratio of the oil product to the slurry is greater than 0.4, the slurry is a secondary raw material that affects the total effective gas production, and the oil product is the main raw material.

[0037] A coupled gasification feeding device and method provided in an embodiment of the present invention adopts a multi-channel burner to meet the feeding requirements of the burner, and proposes a reasonable oxygen-carbon ratio control scheme for different raw material gas production and oxygen consumption in a coupled gasification system of oil products and high-carbon slurry, and proposes a suitable shutdown oil pipeline flushing and cleaning configuration scheme from the perspective of raw material atomization and burner protection. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 Shown is a schematic structural diagram of a coupled gasification feeding device provided in one embodiment of the present invention.

[0039] Figure 2 Shown is a schematic structural diagram of a burner provided in one embodiment of the present invention.

[0040] Figure 3 Shown is a cross-sectional schematic diagram of a burner structure provided by an embodiment of the present invention.

[0041] Figure 4 FIG. 1 is a schematic diagram of a method for adjusting the input ratio of oxygen provided by an embodiment of the present invention.

[0042] Explanation of the reference numerals: 1-slurry feed pump; 2-oil product feed pump; 3-process burner; 4-burner cooling system; 5-gasifier; 101-oxygen; 102-slurry; 103-oil product; 104-high-pressure nitrogen; 105-high-pressure nitrogen; 106-high-pressure steam; 107-burner cooling water supply; 108-burner cooling water return. DETAILED DESCRIPTION

[0043] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0044] The inventor of the present application has found that in the prior art, in order to solve the above problems, the commonly used methods include heavy oil storage and transportation system, coal slurry preparation and transportation system, gasification and synthesis gas washing system, slag cooling and treatment system and ash water treatment system. The main body is configured the same as the traditional water-coal slurry gasification process, and the heavy oil storage and transportation system is added. The process burner used is a four-channel burner, which is arranged from the inside to the outside in sequence, a central tube, a first ring tube, a second ring tube and an outer ring tube. A water cooling mechanism is arranged on the lower outer wall of the outer ring tube. The central tube is hollow to form a central material channel, the first ring tube is hollow to form a primary oxygen channel, the second ring tube is hollow to form an outer material channel, and the outer ring tube is hollow to form a secondary oxygen channel. The bottom of the central tube is flush with the bottom of the first ring tube, and the bottom of the second ring tube is higher than the bottom of the outer ring tube to form a premixing zone. The slurry (heavy oil and coal slurry) and the primary oxygen are premixed once before entering the gasifier, and then enter the furnace together with the secondary oxygen to react. The heavy oil feed pipeline is equipped with superheated steam and nitrogen interfaces. When the feed is stopped, nitrogen is introduced first and then steam to flush and clean the heavy oil pipeline. In order to ensure that the heavy oil temperature is maintained at 60-90°C, the horizontal heavy oil storage tank and related pipelines need to be steam-heated. In order to adapt to the control of the oxygen-carbon ratio during the co-gasification of coal and heavy oil, a kind of heavy oil is converted into an equivalent coal slurry, and then added to the coal slurry flow rate, and correlated with a fixed oxygen-coal ratio coefficient to calculate the total oxygen consumption, which is used as the basis for adjusting the oxygen flow rate. Although this method can theoretically meet the design purpose of the co-gasification of coal and heavy oil, it has the following disadvantages:

[0045] (1) The burner end is provided with a premixing zone for slurry (heavy oil and coal slurry) and primary oxygen. Since the temperature of coal slurry and oxygen is relatively low, and the heavy oil often has a higher operating temperature to meet the problems of transportation and atomization. After mixing with coal slurry and oxygen in the premixing zone, the temperature of the heavy oil will be reduced, affecting the atomization effect of the heavy oil at the burner end, reducing the gasification reaction effect, and in severe cases, the burner head channel may be blocked. In addition, the slurry properties of heavy oil and coal slurry are quite different, and the mixing effect is poor, which makes the stability of the slurry reaction at the burner end worse, affecting the burner life;

[0046] (2) The overall control idea of ​​the oxygen-carbon ratio is to simply associate the coal slurry and heavy oil with a coefficient, and the coefficient is a fixed value of 1.6. The heavy oil flow is converted into an equivalent coal slurry through the coefficient association, and then the oxygen flow required is calculated and adjusted through the set oxygen-coal ratio coefficient. Different coal slurries and heavy oils, heavy oil blending ratios, and coal slurry concentrations will affect the ratio of heavy oil to coal slurry oxygen consumption. Associating with fixed parameters will cause large deviations when the operating conditions change, which will affect the reaction effect and cause problems such as over-oxygenation and furnace overheating. In addition, the control scheme does not explain the adjustment of the oxygen-carbon ratio when the load changes. The idea it provides can only cope with the adjustment of the oxygen-carbon ratio under a fixed load. It does not associate the load with the slurry (heavy oil and coal slurry) and the oxygen flow, and fails to propose a solution to completely solve the oxygen-carbon ratio control in the coal and heavy oil co-gasification system.

[0047] (3) When the system is shut down, nitrogen purge is used first and then steam purge is used, which will cause the heavy oil in the heavy oil feed pipeline to cool and solidify, and the fluidity will deteriorate. Then steam purge will greatly reduce the overall purge cleaning effect and greatly increase the steam consumption. The determination of the heavy oil feed temperature is related to the heavy oil atomization, transportation requirements and burner protection. The specific parameters are mainly viscosity, tension and flash point. If the temperature is controlled at 60-90℃, it is difficult to meet the heavy oil atomization and transportation requirements when processing inferior heavy oil, which affects the stability of the feed system and the reaction effect.

[0048] (4) The inner material channel can simultaneously exchange momentum with the central oxygen channel and the outer oxygen channel for atomization. The outer material channel can only exchange momentum with the outer oxygen channel. In the claims described in the patent, the heavy oil and coal slurry raw materials with a small flow rate go through the inner material channel, while the heavy oil and coal slurry raw materials with a large flow rate go through the outer material channel, which reduces the atomization effect of the raw materials.

[0049] In view of the above problems, the present invention proposes a coupled gasification feeding device and method, which adopts a multi-channel burner to meet the feed requirements of the burner, and proposes an oxygen-carbon ratio control scheme associated with load, raw material feed amount and oxygen feed amount for the gas production and oxygen consumption of different raw materials in the coupled gasification system of oil products and high-carbon slurry, and for the reaction of two different raw materials, to adapt to various control requirements in the coupled gasification system, and proposes a purge scheme for the oil product feed pipeline and the requirements for the oil product feed temperature. See the following embodiment for details.

[0050] In one embodiment of the present invention, a coupled gasification feeding device is provided, such as Figure 1 As shown, the coupled gasification feeding device includes: a gasifier 5, a burner 3, a slurry preparation and delivery system, an oil storage and feeding system, an oxygen supply system and a channel control system. The burner 3 is distributed at the inlet of the gasifier 5, and the burner 3 includes a plurality of channels (such as Figure 2 and Figure 3 As shown); the channel includes a slurry channel, an oil product channel and an oxygen channel; a slurry preparation and delivery system, used to prepare slurry and deliver slurry to the slurry channel; an oil product storage and feeding system, used to store oil products and deliver oil products to the oil product channel; an oxygen supply system, used to provide oxygen and deliver oxygen to the oxygen channel; a channel control system, used to select the slurry channel and the oil product channel from the multiple channels according to the feed amount ratio of the oil product and the slurry. The main process of the coupled gasification feeding device is the slurry 102 from the slurry preparation and delivery system, which enters the slurry channel of the process burner 3 after being pressurized by the slurry feed pump 1. The oil product 103 from the heavy oil storage and feeding system is pressurized by the oil product feed pump 2 and is sent to the oil product channel of the process burner 3. High-purity oxygen 101 from outside enters the oxygen channel of the process burner 3. The slurry, oil products and oxygen enter the gasifier 5 through the coaxial jet of the multi-channel process burner 3 arranged at the top of the gasifier 5 for gasification reaction.

[0051] Optionally, the oil product is heavy oil produced by various units of a refinery, such as one or more of atmospheric residue oil, vacuum residue oil, hydrogenation tail oil, coking tail oil, and ethylene tar.

[0052] Optionally, the slurry is a high carbon content slurry, including a slurry containing coal, petroleum coke, high-concentration organic wastewater, sludge, oil sludge and a mixture thereof.

[0053] The gasifier 5 is a place where feed materials such as slurry and oil products react with a gasifying agent to produce synthesis gas. Optionally, the gasification pressure of the gasifier 5 is normal pressure to 6.5 MPaG; the gasification temperature is 1100°C to 1600°C; the gasifying agent is pure oxygen, high-pressure steam, etc.; the gasifier 5 is a cold wall type or a hot wall type, the cold wall type is a water-cooled wall type, and the hot wall type is a refractory material type.

[0054] In one embodiment of the present invention, Figure 3 As shown, the channel includes a first channel 031 and a second channel 033; the channel control system is configured to select the first channel 031 as the oil channel and the second channel 033 as the slurry channel when the mass ratio of the oil product to the slurry is between 0.02 and 1; when the mass ratio of the oil product to the slurry is greater than 1, the second channel 033 is selected as the oil channel and the first channel 031 is selected as the slurry channel. Optionally, the burner 3 used is a multi-channel burner 3, and the end faces of each channel are flush and there is no premixing zone. According to the different feed amounts of the oil product and the slurry, it is determined whether the two raw materials go through the first channel 031 or the second channel 033 respectively.

[0055] In one embodiment of the present invention, Figure 3As shown, the oxygen channel includes a central oxygen channel 032 and an annular oxygen channel 034; the central oxygen channel 032 is arranged on one side of the second channel 031; the annular oxygen channel 034 is arranged on the side of the second channel 033 away from the central oxygen channel 032, and the first channel 033 is arranged on the side of the annular oxygen channel 032 away from the second channel 031; wherein the central oxygen channel 032 is arranged on the inner side of the burner 3. It can be understood that Figure 2 As shown, on the side wall of the burner, from top to bottom, there are the central oxygen channel 032, the second channel 033, the annular oxygen channel 034 and the first channel 031; inside the burner, from inside to outside, there are the central oxygen channel 032, the second channel 033, the annular oxygen channel 034 and the first channel 031; the material with a large feed mass in the oil product and slurry is fed from the second channel 033. The burner 3 is a multi-channel burner 3, and the burner 3 has the central oxygen channel 032, the first channel 031, the annular oxygen channel 034 and the second channel 033 from inside to outside. The high-purity oxygen 101 from outside enters the burner 3 and is divided into two paths, entering the central oxygen channel 032 and the annular oxygen channel 034 of the process burner 3 respectively. The oxygen flow rates of the central oxygen channel 032 and the annular oxygen channel 034 are distributed by means of a throttling element. Usually, the ratio of oxygen introduced into the central oxygen channel 032 and the annular oxygen channel 034 is 1:19 to 1:3.

[0056] In one embodiment of the present invention, when the ratio of oil product to slurry is greater than 0.4, the channel also includes a protective channel, which is arranged between the oil product channel and the oxygen channel. When the oil product feed amount is dominant, in order to ensure the atomization of the oil product, the black area at the burner 3 outlet and the water required for the reaction, a high-pressure steam channel can be added between the annular oxygen channel 034 and the oil product channel. In order to ensure the transportation and atomization of the oil product, the oil product related equipment and pipelines are heated by steam to maintain the oil product at a certain temperature. The oil product temperature is a comprehensive consideration of multiple factors such as oil product atomization, transportation, thermal stability and flash point. The temperature of the feed oil product varies according to the properties of the oil product. Optionally, the viscosity of the feed oil product needs to be controlled to be no more than 500cp and at least 20°C lower than the flash point. Generally, the oil product feed temperature is between 50°C and 350°C.

[0057] In one embodiment of the present invention, the coupled gasification feeding device further comprises: an oxygen-carbon ratio control system for adjusting the input ratio of oxygen. The specific adjustment method is described in the following embodiment.

[0058] In one embodiment of the present invention, the coupled gasification feeding device further includes: a cooling system 4, which is arranged on the burner 3 and is used to cool down and protect the burner 3. The process burner 3 is provided with a cooling system 4, which cools down and protects the burner 3 by circulating cooling water. The burner 3 cooling water supply water 107 enters from the inlet of the cooling system 4, and the burner 3 cooling water return water 108 is discharged from the outlet of the cooling system 4. Optionally, the burner 3 cooling system 4 can be a jacket type or a coil type.

[0059] In one embodiment of the present invention, the coupled gasification feeding device further includes: a high-pressure purge system, which is arranged at the channel of the burner 3 and is used to purge and flush the channel. Optionally, the high-pressure purge system includes a superheated steam purge pipeline and a high-pressure nitrogen purge pipeline. Optionally, the steam pipeline connected to the oil product has a purge flow rate of 3 to 15 m / s when the oil product pipeline is purged and cleaned when the oil product stops feeding; the oil product channel is provided with a high-pressure superheated steam 106 purge pipeline interface, and the oxygen and slurry pipelines are provided with independent high-pressure nitrogen purge pipeline (104 and 105) interfaces. When the gasification system is stopped, high-pressure steam and nitrogen are used to purge and flush the oil product, slurry and oxygen pipelines, and reverse flow of the synthesis gas is prevented.

[0060] In one embodiment of the present invention, a limit controller is also included to adjust the flow rate of slurry and oil product.

[0061] In one embodiment of the present invention, a coupled gasification feeding method is provided, comprising:

[0062] Step 001: selecting a slurry channel and an oil channel from multiple channels according to the feed ratio of the oil product and the slurry;

[0063] Step 002: transport the slurry to the slurry channel, transport the oil product to the oil product channel, and transport the oxygen to the oxygen channel.

[0064] In one embodiment of the present invention, the coupled gasification feeding method further includes: adjusting the input ratio of oxygen, that is, adjusting the oxygen-carbon ratio. When adjusting the oxygen-carbon ratio, it is necessary to fix the flow rate of one raw material and adjust the flow rates of the two raw materials one by one to the target value. When increasing or decreasing the load, there are various requirements for the actual production of raw material adjustment. One is that the two raw materials are adjusted in the same proportion, the second is that the two raw materials are adjusted according to their respective proportions, and the third is that one raw material is fixed and only the other raw material is adjusted. From the perspective of system stability, no matter what the requirement is, one raw material is fixed and the other raw material is adjusted to the target value first, and then the fixed raw material is adjusted. The system has the best stability and is most suitable for the gasification of multi-carbon material systems.

[0065] Load increase operation. The oil flow rate remains unchanged, and the required slurry flow rate is determined by calculation. The required slurry flow rate determined by calculation will be combined with the measured slurry flow rate in the low selector to select the lower value as the input value of the multiplication calculator, so as to determine the oxygen flow rate required for the slurry. Then, the slurry flow rate can be obtained by dividing the difference between the actual flow rate of the oxygen pipeline and the oxygen flow rate required for the oil gasification calculation with the oxygen / slurry set value. The slurry flow rate calculated by the load and the slurry flow rate calculated by the oxygen-slurry ratio, after the two flow signals are calculated in the high selector, the higher value is selected as the set value of the slurry flow rate and sent to the regulator. In this way, when the load is increased, the control purpose of increasing the slurry load first and then increasing the oxygen can be achieved.

[0066] Load reduction operation. The oil product flow remains unchanged, and the required slurry flow is determined by calculation. The oxygen flow required for slurry gasification determined by calculation will be selected in the low selector with the measured slurry flow, and finally the load-calculated slurry flow will be selected as the input value of the multiplication calculator. Then, a slurry flow can be obtained by dividing the difference between the actually measured flow of the oxygen pipeline and the oxygen flow required for the oil product gasification calculation by the set value of the oxygen-coal ratio. The higher value of the slurry flow calculated by the oxygen-slurry ratio and the flow signal calculated by the load after high selection is used as the input value for slurry flow adjustment. The slurry flow calculated by the oxygen-slurry ratio and the slurry flow calculated by the load change in the same amplitude, which can achieve the control purpose of reducing oxygen first and then reducing coal.

[0067] In one embodiment of the present invention, adjusting the oxygen input ratio includes:

[0068] Step 0011: based on the first raw material feed amount, the second raw material feed amount and the reaction temperature, obtain the total effective gas production and total oxygen consumption under oil-coal coupled gasification;

[0069] Step 0012: fixing the reaction temperature and the feed amount of the second raw material, determining the effective gas production and oxygen consumption of the second raw material reaction, and obtaining the effective gas production and oxygen consumption of the first raw material based on the total effective gas production and total oxygen consumption, and the effective gas production and oxygen consumption of the second raw material reaction;

[0070] Step 0013: Determine the unit effective gas production and unit oxygen consumption of the first raw material and the second raw material based on the first raw material feed amount, the second raw material feed amount, the first raw material effective gas production and oxygen consumption, and the second raw material effective gas production and oxygen consumption;

[0071] Step 0014: Under a preset gas production load, the total effective gas production and the first effective gas production, determine the main raw material and the secondary raw material that affect the total effective gas production from the first raw material and the second raw material;

[0072] Step 0015: fixing the flow rate of the main raw material, adjusting the flow rate of the secondary raw material to a first target flow rate value, and in the adjustment process, obtaining the oxygen consumption of the secondary raw material flow rate and the oxygen consumption of the main raw material based on the unit oxygen consumption of the main raw material and the unit oxygen consumption of the secondary raw material;

[0073] Step 0016: Obtaining a first total oxygen demand based on the oxygen consumption of the secondary raw material and the oxygen consumption of the primary raw material;

[0074] Step 0017: After the flow rate of the secondary raw material is adjusted to the first target flow rate value, the flow rate of the secondary raw material is fixed, and under a preset gas production load, a second target flow rate value of the main raw material is obtained based on the total effective gas production, the adjusted flow rate of the secondary raw material, and the unit effective gas production of the secondary raw material, and the flow rate of the main raw material is adjusted to the second target flow rate value;

[0075] Step 0018 Step 0014: During the adjustment process, the oxygen consumption corresponding to the main raw material and the oxygen consumption corresponding to the secondary raw material under the preset gas production load are obtained from the unit oxygen consumption of the main flow and the unit oxygen consumption of the secondary raw material;

[0076] Step 0019: Obtaining a second total oxygen demand based on the oxygen consumption of the secondary raw material flow and the oxygen consumption of the primary raw material;

[0077] Step 0020: Adjust the oxygen input ratio based on the first total oxygen demand and the second total oxygen demand.

[0078] Specifically, under any gas production load, based on the total effective gas production under the load and the requirements for the first raw material processing volume, determine the main raw material and the secondary raw material that affect the total effective gas production among the first raw material and the second raw material. First, fix the flow rate of the main raw material, adjust the flow rate of the secondary raw material to the target value, and during the adjustment process, calculate the oxygen consumption corresponding to the flow rate of any secondary raw material and the oxygen consumption of the main raw material from the unit raw material oxygen consumption of the two raw materials, and the sum of the two is the total oxygen demand; after the flow rate of the secondary raw material is adjusted to the target value, fix the flow rate of the secondary raw material, and obtain the target flow rate of the main raw material based on the total effective gas production under any load, the adjusted flow rate of the secondary raw material, and the unit effective gas production of the secondary raw material, and adjust the main raw material to the target flow rate. During the adjustment process, obtain the oxygen consumption corresponding to any main raw material and the oxygen consumption of the secondary raw material from the unit oxygen consumption of the two raw materials, and the sum of the two is the total oxygen demand;

[0079] adjusting the oxygen input ratio based on the total oxygen demand in the two processes;

[0080] Step 0015: Adjust the oxygen input ratio based on the total oxygen demand.

[0081] Among them, when the mass ratio of the oil product to the slurry is between 0.02 and 1, the first raw material is the oil product and the second raw material is the slurry; when the mass ratio of the oil product to the slurry is greater than 1, the first raw material is the slurry and the second raw material is the oil product.

[0082] Among them, when the mass ratio of the oil product to the slurry is between 0.02 and 0.4, the oil product is a secondary raw material affecting the total effective gas production, and the slurry is the main raw material. When the mass ratio of the oil product to the slurry is greater than 0.4, the slurry is a secondary raw material affecting the total effective gas production, and the oil product is the main raw material.

[0083] In this embodiment, oil products are taken as the secondary raw material that affects the total effective gas production as an example to explain the load adjustment; when the slurry flow is the secondary raw material, the method is the same and will not be repeated here.

[0084] Among them, Figure 4 As shown, the adjusting the oxygen input ratio comprises:

[0085] Step 0021: Based on the slurry feed rate, oil product feed rate and reaction temperature, the total effective gas production and total oxygen consumption under oil-coal coupled gasification are obtained.

[0086] Firstly, the total effective gas production and total oxygen consumption under the coupled gasification of oil product and slurry are determined according to the slurry feed rate, oil product feed rate and the determined reaction temperature.

[0087] Step 0022: Fix the reaction temperature and the slurry feed rate, determine the effective gas production and slurry oxygen consumption of the slurry reaction, and obtain the effective gas production and oxygen consumption of the oil product based on the total effective gas production and total oxygen consumption, the effective gas production and oxygen consumption of the slurry reaction.

[0088] Fixed reaction temperature and slurry feed rate, determine the effective gas production and oxygen consumption of slurry reaction, subtract the two to get the effective gas production and oxygen consumption of oil products. The unit effective gas production and unit oxygen consumption of the two raw materials can be obtained from the slurry and oil product feed rates. The four determined parameters are used as the basic parameters of the oxygen-carbon ratio control scheme.

[0089] A=α*X+β*Y

[0090] B=λ*X+θ*Y

[0091] In the formula: A is oxygen flow rate, Nm3 / h, B is effective gas production, Nm3 / h, X is slurry flow rate, m3 / h, Y is oil flow rate, kg / h, α is unit slurry oxygen consumption, Nm3 / m3, β is unit oil oxygen consumption, Nm3 / kg, λ is unit slurry effective gas production, Nm3 / m3, θ is unit oil effective gas production, Nm3 / kg.

[0092] Optionally, the oxygen consumption per unit slurry α is 300-550, the oxygen consumption per unit oil product β is 0.4-0.8, the effective gas production per unit slurry λ is 1100-1500, and the effective gas production per unit oil product θ is 1.8-4.0.

[0093] Optionally, the mass ratio of the oil product to the slurry is between 0.02 and 0.4. When adjusting the load, the slurry flow rate is first fixed, and the oil product flow rate is adjusted to the target flow rate of the actual processing requirement, and then the slurry flow rate is adjusted to the target flow rate while fixing the oil product flow rate; when it is greater than 0.4, when adjusting the load, the oil product flow rate is first fixed, and the slurry flow rate is adjusted to the target flow rate of the actual processing requirement, and then the slurry flow rate is adjusted to the target flow rate while fixing the oil product flow rate. Figure 4 The control principle diagram shown is for the scheme of adjusting the oil first and then adjusting the slurry. If the scheme is to adjust the slurry first and then the oil, Figure 4 The medium slurry and heavy oil can be interchanged.

[0094] Step 0023: According to the heavy oil processing capacity requirement, the heavy oil flow rate is first adjusted to the target value. During the adjustment process, the heavy oil flow rate is limited by a range controller to ensure that the heavy oil flow rate is adjusted within a reasonable and safe range. The intermediate flow rate is obtained, and the oxygen flow rate required for slurry gasification and the oxygen flow rate required for oil product gasification are obtained based on the heavy oil flow rate, the effective gas production of the oil product, the effective gas production of the slurry, the slurry oxygen consumption and the oil product oxygen consumption.

[0095] Specifically, the heavy oil flow measured by the oil flow meter passes through the three-centering module to select the middle value, and then the θ determined in step A is calculated in the multiplication calculator to calculate the oil gas production; the gas production load required by the slurry is calculated by subtracting the oil gas production in the subtraction calculator; after determining the slurry gas production load, it is divided by the slurry gas production coefficient λ in the divider to determine the required slurry flow; the required slurry flow is calculated and the actual slurry flow after three-centering is selected in the low selector. The value is then run in the multiplier with the oxygen / slurry flow α to calculate the oxygen flow required for slurry gasification; the required slurry flow and the actual slurry flow after three-centering are selected in the low selector. The value is then run in the multiplier with the oxygen / slurry flow α to calculate the oxygen flow required for slurry gasification.

[0096] Step 0024: Obtain a total oxygen demand based on the oxygen flow rate required for the slurry gasification and the oxygen flow rate required for the oil product gasification; calculate the total oxygen demand after the oxygen flow rate required for the slurry gasification and the oxygen flow rate required for the oil product gasification are calculated in an adder.

[0097] Step 0025: Adjust the oxygen input ratio based on the total oxygen demand. The total oxygen demand is used as the set value of the oxygen regulating valve, and compared with the measured oxygen flow rate as the input value of the oxygen regulating valve.

[0098] In one embodiment of the present invention, in response to the problems existing in the prior art, the present invention proposes a feeding method and an oxygen-carbon ratio control scheme suitable for a coupled gasification system of oil products and high-carbon slurry. The burner 3 structure can not only meet the requirements of raw material atomization, but also avoid the problems of heavy oil cooling and solidification in the premixing zone and uneven premixing affecting the reaction in the comparative patent; the two raw materials of oil products and slurry, the one with a larger flow rate goes through the inner material channel, which can be more conducive to the atomization of the raw materials; the basic parameters of the proposed oxygen-carbon ratio control scheme are related to the material properties of the slurry and the oil products, and factors such as the oil product blending ratio are also related. Compared with the simple equivalent coal slurry conversion of the comparative patent, it is more suitable for the co-gasification of slurry and oil products; in addition, this patent takes into account the analysis of oxygen-carbon ratio adjustment when the load changes, and the ideas provided can not only cope with the adjustment of oxygen-carbon ratio under fixed load, but also realize the correlation between load and carbon-containing raw materials (oil products and slurry) and oxygen flow rate. It is a more complete solution for controlling the oxygen-carbon ratio of co-gasification of slurry and oil products; the oil pipeline purge and flushing solution proposed in this patent can avoid solidification of the oil pipeline during shutdown, and can also reduce the consumption of purge steam compared with the comparative patent.

[0099] Optionally, the technical concept of the oil and slurry coupled gasification feeding device and method provided by the present invention has no restrictions on the type of gasification raw materials, the size, shape, and internal parts of the equipment, and any changes to one or more of the above configurations of the gray water treatment system cannot circumvent the constraints of this patent.

[0100] In one embodiment of the present invention, taking a certain type of coal and tail oil of a residual oil hydrogenation unit as an example, the specific research is as follows:

[0101] (1) Raw material specifications

[0102] Table 1 Raw coal specifications

[0103]

[0104] Table 2 Specifications of residue hydrotreating tail oil

[0105]

[0106]

[0107] (2) Scale

[0108] The coal / oil coupled gasification has a single furnace effective gas production of ~100,000 Nm3 / h, the concentration of water-coal slurry is 62wt%, the reaction pressure of the gasifier is 6.5MPaG, the furnace temperature is 1280℃, the tail oil flow rate in the coal / oil coupled gasification is 15000kg / h, the tail oil feed temperature is 250℃, and the coal slurry feed amount is 52090kg / h.

[0109] (3) Feeding system solution

[0110] The feed mass ratio of heavy oil to coal slurry is 0.288. Because it is less than 0.4, the burner adopts a four-channel structure, and no steam protection channel is set. The heavy oil goes through the outer logistics channel and the coal slurry goes through the inner logistics channel. The total oxygen consumption is 31465Nm3 / h, and the central oxygen channel is controlled at 5660~6295Nm3 / h, accounting for about 18%~20% of the total oxygen. The burner adopts coil cooling.

[0111] (4) Determination of oxygen-carbon ratio control scheme

[0112] By calculating the oxygen consumption and effective gas production under oil-coal coupling conditions, as well as the oxygen consumption and effective gas production under full coal conditions, the four basic parameters of oxygen-carbon ratio control are determined.

[0113] 1) Oxygen consumption coefficient per unit raw material

[0114] Table 3 Coal / Oil Coupled Gasification Oxygen Consumption (100% Operating Condition)

[0115] project Coal / Oil Coupled Gasification Full coal gasification Oven temperature ℃ 1280 1280 <![CDATA[Oxygen consumption Nm 3 / h]]> 31465 22030 Dry basis coal feed rate kg / h 32996 32996 <![CDATA[Coal slurry flow rate m 3 / h]]> 44.35 44.35 Heavy oil feed rate kg / h 15000 -- <![CDATA[Oxygen consumption per unit mass of raw material Nm 3 / kg dry basis]]> 0.6677

[0116] It is concluded that α is 496.73Nm3 / m3, β is 0.66Nm3 / kg, and the oxygen consumption formula is as follows:

[0117] A=496.73*X+0.66*Y

[0118] Verify under multiple load conditions

[0119] Table 4 Raw material and oxygen consumption under different gas production loads

[0120] project 60% load 90% load 120% load Oven temperature ℃ 1280 1280 1280 <![CDATA[Effective gas production Nm 3 / h]]> 59957 90040 119951 Dry basis coal feed rate kg / h 10917 27382 44159 <![CDATA[Coal slurry flow rate m 3 / h]]> 14.67 36.80 59.35 Heavy oil feed rate kg / h 15000 15000 15000 <![CDATA[Calculating oxygen consumption Nm 3 / h]]> 16850 27720 38900 <![CDATA[Coefficient of association calculation for oxygen consumption Nm 3 / h]]> 17187 28180 39380 <![CDATA[Difference in oxygen consumption between two methods, Nm 3 / h]]> 337 460 480 Error between the two calculation methods% 1.96 1.63 1.22

[0121] The errors of the oxygen consumption calculated by simulation under three loads and that calculated by correlation formula are all within 2%, which is acceptable in engineering design.

[0122] 2) Unit raw material effective gas production coefficient

[0123] Table 5 Coal / Oil Coupled Gasification Oxygen Consumption (100% Operating Condition)

[0124] project Coal / Oil Coupled Gasification Full coal gasification Full oil gasification Oven temperature ℃ 1280 1280 1280 <![CDATA[Effective gas production Nm 3 / h]]> 100066 58416 41650 Dry basis coal feed rate kg / h 32996 32996 -- <![CDATA[Coal slurry flow rate m 3 / h]]> 44.35 44.35 -- Heavy oil feed rate kg / h 15000 -- 15000 <![CDATA[Effective gas volume per unit mass of raw material Nm 3 / kg dry basis]]> -- 1.77 2.78

[0125] It is concluded that λ is 1317Nm3 / m3, θ is 2.786Nm3 / kg, and the effective gas production formula is as follows:

[0126] B=1317*X+2.78*Y

[0127] Verify under multiple load conditions.

[0128] Table 6 Raw material and effective gas production under different gas production loads

[0129] project 60% load 90% load 120% load Oven temperature ℃ 1280 1280 1280 <![CDATA[Oxygen consumption Nm 3 / h]]> 16850 27720 38900 Dry basis coal feed rate kg / h 10917 27382 44159 <![CDATA[Coal slurry flow rate m 3 / h]]> 14.67 36.80 59.35 Heavy oil feed rate kg / h 15000 15000 15000 <![CDATA[Calculate the effective gas production Nm 3 / h]]> 59957 90040 119951 <![CDATA[Calculation of correlation coefficient for effective gas production Nm 3 / h]]> 61020 90166 119864 <![CDATA[Difference in effective gas production between two methods, Nm 3 / h]]> 1063 126 -87 Error between the two calculation methods% 1.74 0.01 0.00

[0130] The errors between the effective gas production calculated by simulation under three loads and that calculated by correlation formula are all within 2%, which is acceptable in engineering design.

[0131] The mass ratio of heavy oil to coal slurry feed is 0.288, which is less than 0.4, so a regulation scheme with fixed heavy oil flow rate is adopted.

[0132] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A coupled gasification feeding device, characterized in that: include: Gasifier; A burner is disposed at the inlet of the gasifier, and the burner includes a plurality of channels; the channels include a slurry channel, an oil channel and an oxygen channel; A slurry preparation and delivery system, used for preparing slurry and delivering the slurry to a slurry channel; Oil storage and feeding system, used to store oil and transport oil to oil channels; an oxygen supply system for supplying oxygen and delivering the oxygen to the oxygen passage; The channel control system is used to select the slurry channel and the oil channel from the multiple channels according to the feed ratio of the oil product and the slurry.

2. The coupled gasification feeding device according to claim 1, characterized in that: The channel includes a first channel and a second channel; the channel control system is configured to select the first channel as the oil channel and the second channel as the slurry channel when the mass ratio of the oil product to the slurry is between 0.02 and 1; When the mass ratio of the oil product to the slurry is greater than 1, the second channel is selected as the oil product channel, and the first channel is selected as the slurry channel.

3. The coupled gasification feeding device according to claim 2, characterized in that: The oxygen channel includes a central oxygen channel and an annular oxygen channel; the central oxygen channel is arranged on one side of the second channel; the annular oxygen channel is arranged on a side of the second channel away from the central oxygen channel, and the first channel is arranged on a side of the annular oxygen channel away from the second channel; wherein the central oxygen channel is arranged on the inner side of the burner.

4. The coupled gasification feeding device according to claim 2, characterized in that: When the mass ratio of the oil product to the slurry is greater than 0.4, the channel further includes a protection channel, which is arranged between the oil product channel and the oxygen channel.

5. The coupled gasification feeding device according to claim 1, characterized in that: Also includes: Oxygen-carbon ratio control system is used to adjust the oxygen input ratio.

6. The coupled gasification feeding device according to claim 1, characterized in that: Also includes: The cooling system is arranged on the burner and is used for cooling and protecting the burner.

7. The coupled gasification feeding device according to claim 1, characterized in that: Also includes: A high-pressure purge system is arranged at the channel of the burner and is used for purging and flushing the channel.

8. A coupled gasification feeding method, characterized in that: include: According to the feed ratio of oil product and slurry, a slurry channel and an oil product channel are selected from multiple channels; The slurry is transported to the slurry channel, the oil product is transported to the oil product channel, and the oxygen is transported to the oxygen channel.

9. The coupled gasification feeding method according to claim 8, characterized in that: Also includes: Adjust the oxygen input ratio.

10. The coupled gasification feeding method according to claim 9, characterized in that: The step of adjusting the oxygen input ratio comprises: Based on the first raw material feed amount, the second raw material feed amount and the reaction temperature, the total effective gas production and the total oxygen consumption under the oil-coal coupled gasification are obtained; The reaction temperature and the feed amount of the second raw material are fixed, the effective gas production and oxygen consumption of the second raw material reaction are determined, and the effective gas production and oxygen consumption of the first raw material are obtained based on the total effective gas production and total oxygen consumption, the effective gas production and oxygen consumption of the second raw material reaction; Determine the unit effective gas production and unit oxygen consumption of the first raw material and the second raw material based on the first raw material feed amount, the second raw material feed amount, the first raw material effective gas production and oxygen consumption, and the second raw material effective gas production and oxygen consumption; Under a preset gas production load, based on the total effective gas production, determining a main raw material and a secondary raw material that affect the total effective gas production from the first raw material and the second raw material; The flow rate of the main raw material is fixed, and the flow rate of the secondary raw material is adjusted to a first target flow rate value. During the adjustment process, based on the unit oxygen consumption of the main raw material and the unit oxygen consumption of the secondary raw material, the oxygen consumption of the secondary raw material flow rate and the oxygen consumption of the main raw material are obtained; obtaining a first total oxygen demand based on the oxygen consumption of the secondary raw material and the oxygen consumption of the primary raw material; After the flow rate of the secondary raw material is adjusted to the first target flow rate value, the flow rate of the secondary raw material is fixed, and under a preset gas production load, a second target flow rate value of the main raw material is obtained based on the total effective gas production, the adjusted flow rate of the secondary raw material, and the unit effective gas production of the secondary raw material, and the flow rate of the main raw material is adjusted to the second target flow rate value; During the adjustment process, the oxygen consumption corresponding to the main raw material and the oxygen consumption corresponding to the secondary raw material under the preset gas production load are obtained from the unit oxygen consumption of the main flow and the unit oxygen consumption of the secondary raw material; Obtaining a second total oxygen demand based on the oxygen consumption of the secondary raw material flow and the oxygen consumption of the primary raw material; The input ratio of oxygen is adjusted based on the first total oxygen demand and the second total oxygen demand.

11. The coupled gasification feeding method according to claim 9, characterized in that: include: When the mass ratio of the oil product to the slurry is between 0.02 and 1, the first raw material is the oil product and the second raw material is the slurry; When the mass ratio of the oil product to the slurry is greater than 1, the first raw material is the slurry, and the second raw material is the oil product.

12. The coupled gasification feeding method according to claim 10, characterized in that: include: When the mass ratio of the oil product to the slurry is between 0.02 and 0.4, the oil product is the secondary raw material and the slurry is the primary raw material; When the mass ratio of the oil product to the slurry is greater than 0.4, the slurry is the secondary raw material and the oil product is the main raw material.

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