Heat exchange system of submerged combustion type gasifier

Abstract

The invention discloses a heat exchange system of a submerged combustion type gasifier. The system comprises a water bath pool, an overflow port, an overflow weir and a flue gas bubbler, wherein the overflow port is formed in the water bath pool, and the height difference between the overflow weir and the overflow port ranges from 400 mm to 500 mm; and the distance between the bottom of the flue gas bubbler and the bottom of the water bath pool ranges from 190 mm to 210 mm.

Description

Technical Field

[0001] This text relates to the technical field of liquefied natural gas, and particularly refers to a heat exchange system of a submerged combustion vaporizer. Background Art

[0002] An SCV (submerged combustion vaporizer) uses natural gas as fuel. The high-temperature flue gas generated by the combustion of natural gas through a burner directly enters the water bath to heat the water. The liquefied natural gas flows through the heat exchange tube bundle submerged in the water bath and is heated and vaporized by the hot water.

[0003] Since the submerged combustion vaporizer is not affected by seawater and atmospheric temperature, it can be quickly ignited and started, and can be quickly adjusted within the load range of 10%-100%. It is particularly suitable for emergency peak shaving and winter supply guarantee in LNG receiving stations or peak shaving stations. Summary of the Invention

[0004] The inventors of the present application have found that:

[0005] At present, the burners used in SCV submerged combustion vaporizers operating in LNG receiving stations or peak shaving stations are imported. The fuel natural gas and air burn in the burner, and the blower passes the high-temperature flue gas after combustion through the bubbler into the water bath pool to directly contact and exchange heat with the water. A large number of bubbles violently stir the water bath. The existence of overheated bubbles not only increases the contact area between the gas-liquid two phases, but also enhances the convective heat transfer effect between the two-phase mixture near the wall surface and the tube wall, promoting the heat transfer between the gas and water, and the water is heated to a certain temperature. The LNG heat exchange tube bundle is placed below the liquid level of the water bath pool. The gas-water mixture in the water bath pool also generates an upward effect. Under the restriction of the cofferdam, a bottom-up circulating flow is formed outside the heat exchange tube, strengthening the heat exchange between the water and the tube bundle. The liquefied natural gas in the tube is heated and vaporized and superheated to the required export temperature. After the high-temperature flue gas is sprayed into the water bath, the temperature drops rapidly. The water bath absorbs the heat of the flue gas and quickly transfers the heat to the LNG in the tube. Eventually, except for a certain high-temperature area near the flue gas bubbler, the temperature of the rest of the water bath is basically constant.

[0006] In view of the above problems, the present application provides a heat exchange system of a submerged combustion vaporizer. Regarding the bubbling heat exchange between the flue gas and the water and the heat exchange between the water and the LNG coil, by setting a certain height difference between the overflow weir and the overflow port; and setting a reasonable distance between the bottom of the flue gas bubbler and the bottom of the water bath pool, a heat exchange effect with high heat exchange efficiency, low water bath temperature, and high overall thermal efficiency can be achieved.

[0007] In a first aspect, the present application provides a heat exchange system of a submerged combustion vaporizer, the system includes: a water bath pool, an overflow port, an overflow weir, and a flue gas bubbler;

[0008] Among them, the overflow port is arranged on the water bath pool, and the height difference between the overflow weir and the overflow port ranges from 400 to 500 mm; the distance between the bottom of the flue gas bubbler and the bottom of the water bath pool ranges from 190 to 210 mm.

[0009] Compared with the related art, the present application provides a heat exchange system for an immersion combustion gasifier, and the system includes: a water bath pool, an overflow port, an overflow weir, and a flue gas bubbler; among them, the overflow port is arranged on the water bath pool, and the height difference between the overflow weir and the overflow port ranges from 400 to 500 mm; the distance between the bottom of the flue gas bubbler and the bottom of the water bath pool ranges from 190 to 210 mm. By setting a suitable height difference between the overflow weir and the overflow port; and setting a reasonable distance between the bottom of the flue gas bubbler and the bottom of the water bath pool, the system can achieve a heat exchange effect with high heat exchange efficiency, low water bath temperature, and high overall thermal efficiency.

[0010] Other features and advantages of the present application will be described in the subsequent specification, and, in part, will become apparent from the specification, or will be understood by implementing the present application. Other advantages of the present application can be achieved and obtained through the solutions described in the specification and the drawings. Description of the Drawings

[0011] The drawings are used to provide an understanding of the technical solutions of the present application, and constitute a part of the specification. They are used together with the embodiments of the present application to explain the technical solutions of the present application, and do not constitute a limitation to the technical solutions of the present application.

[0012] Figure 1 It is a schematic diagram of the heat exchange system of the immersion combustion gasifier according to the embodiment of the present application. Detailed Embodiments

[0013] The present application describes multiple embodiments, but the description is exemplary rather than restrictive, and it is obvious to those of ordinary skill in the art that there can be more embodiments and implementation solutions within the scope of the embodiments described in the present application. Although many possible combinations of features are shown in the drawings and discussed in the detailed embodiments, many other combination ways of the disclosed features are also possible. Unless specifically restricted, any feature or element of any embodiment can be combined with any other feature or element in any other embodiment, or can replace any other feature or element in any other embodiment.

[0014] This application includes and contemplates combinations with features and elements known to those of ordinary skill in the art. The disclosed embodiments, features, and elements of this application can also be combined with any conventional features or elements to form a unique inventive solution defined by the claims. Any feature or element of any embodiment can also be combined with features or elements from other inventive solutions to form another unique inventive solution defined by the claims. Therefore, it should be understood that any feature shown and / or discussed in this application can be implemented alone or in any suitable combination. Thus, the embodiments are not subject to other limitations except those imposed by the appended claims and their equivalents. In addition, various modifications and changes can be made within the scope of the appended claims.

[0015] In addition, when describing representative embodiments, the specification may have presented the method and / or process as a particular sequence of steps. However, to the extent that the method or process does not depend on the particular order of the steps described herein, the method or process should not be limited to the described particular order of steps. As will be understood by those of ordinary skill in the art, other step orders are possible. Therefore, the particular order of steps set forth in the specification should not be construed as a limitation on the claims. In addition, the claims directed to the method and / or process should not be limited to performing their steps in the order written, and those skilled in the art can readily understand that these orders can vary and still remain within the spirit and scope of the embodiments of this application.

[0016] The bubbling heat transfer between flue gas and water and the heat transfer between water and the LNG coil are the keys to the design and manufacture of SCV vaporizers. The existing heat exchange systems of imported SCVs have the following problems:

[0017] 1. The flow rate of LNG at the tube side inlet is relatively low, the heat transfer coefficient at the tube side is relatively small, and the heat transfer area is relatively large, resulting in a relatively high one-time investment.

[0018] 2. The flue gas volume in the water bath is relatively small, that is, the air volume in the upstream combustion system is relatively small, and the air excess coefficient is relatively small, resulting in weak disturbance outside the tubes and a relatively small heat transfer coefficient.

[0019] 3. The initial liquid level height, that is, the height difference between the overflow weir and the overflow outlet of the water bath. If the initial liquid level is too high, severe liquid droplets splashing occurs inside the device, causing water loss in the water bath and resulting in unstable operation of the SCV.

[0020] 4. The immersion depth of the flue gas bubbler is relatively shallow, which cannot fully ensure the stability of the heat transfer turbulence above the tube bundle, resulting in an excessively low heat transfer coefficient outside the tubes.

[0021] 5. The opening ratio of the flue gas bubbler is relatively low, resulting in a relatively low heat transfer coefficient outside the tubes.

[0022] In view of the above problems, the inventors of the present application propose a heat exchange system for a submerged combustion gasifier, which can fully achieve the heat exchange design goals of small heat exchange area, high heat exchange efficiency, low water bath temperature, and high overall thermal efficiency.

[0023] An embodiment of the present invention provides a heat exchange system for a submerged combustion gasifier, as Figure 1 shown, the system includes: a water bath pool, an overflow port, an overflow weir, and a flue gas bubbler;

[0024] Wherein, the overflow port is arranged on the water bath pool, and the height difference between the overflow weir and the overflow port ranges from 400 to 500 mm; the distance between the bottom of the flue gas bubbler and the bottom of the water bath pool ranges from 190 to 210 mm.

[0025] In an exemplary embodiment, as Figure 1 shown, the heat exchange system of the submerged combustion gasifier includes: a water bath pool 1, an overflow port 2, an overflow weir 3, a heat exchange coil 4, a main fan 5, a flue gas bubbler 6, openings 7 in the upper part of the bubbler, and a combustion chamber 8.

[0026] Wherein: A certain amount of water is contained in the water bath pool 1 to reach a certain liquid level line. The water bath pool 1 is provided with an overflow port 2. The height difference between the overflow weir 3 and the overflow port 2 of the water bath pool is used as the initial liquid level. Part of the combustion chamber 8, part of the overflow weir 3, all of the flue gas bubbler 6, and all of the heat exchange coil 4 are submerged in water. A reasonable distance range is set between the bottom of the flue gas bubbler 6 and the bottom of the water bath pool: 190 to 210 mm. A number of openings 7 are provided in the upper part of the flue gas bubbler 6.

[0027] In an exemplary embodiment, the preset height difference between the overflow weir and the overflow port ranges from 450±50 mm, that is, 400 to 500 mm. The height of the overflow port is used as the initial liquid level. In this embodiment, the initial liquid level height, that is, the height difference between the overflow weir and the overflow port of the water bath pool, ensures the heat exchange speed of the water bath flow channel. Given that the initial liquid level height is too low, that is, the height difference is too high, the two-phase overflow amount decreases or even disappears, and an effective overflow cannot be formed, that is, an effective circulation disturbance cannot be formed, resulting in the abnormal operation of the SCV; if the initial liquid level is too high, that is, the height difference is too low, the liquid foam splashing in the device is serious, causing water loss in the water bath pool, which is not conducive to the normal operation of the SCV. The liquid foam splashing in the device is serious, causing water loss in the water bath pool, which is not conducive to the normal operation of the SCV.

[0028] Take the height difference of 450 ± 50 mm between the overflow weir and the overflow outlet of the water bath as the optimal initial liquid level. Determine the initial liquid level according to the experiment. The experimental data show that: (1) When the height difference between the overflow weir and the overflow outlet of the water bath is 390 mm, that is, the initial liquid level is too high. After testing, the liquid foam splash height in the device reaches 570 mm, exceeding the height of the overflow weir plate by 120 mm, causing water loss in the water bath. After running for 30 minutes and stopping for testing, the initial liquid level drops by 16 mm, which is not conducive to the normal operation of the SCV. (2) When the height difference between the overflow weir and the overflow outlet of the water bath is 510 mm, that is, the initial liquid level is too low. It is found that the two-phase overflow rate is 0, and no effective overflow is formed, that is, no effective circulating disturbance can be formed. At this time, the heat transfer coefficient of the water bath decreases by 40%. The theoretical temperature of the medium in the heat exchange tube should be -5°C, but the experimental value is only -25°C, indicating that the medium in the heat exchange tube does not exchange heat well and the SCV fails to operate normally.

[0029] (3) When the height difference between the overflow weir and the overflow outlet of the water bath is 400 mm, after testing, the liquid foam splash height in the device reaches 550 mm, exceeding the height of the overflow weir plate by 100 mm. The overflow water flows back into the overflow weir from the same part at the lower part of the overflow weir to form a fierce circulating water; after calculation, the heat transfer coefficient of the water bath is consistent with the theoretical value. The theoretical temperature of the medium in the heat exchange tube should be -5°C, and the experimental value is -4°C, indicating that the SCV can operate normally.

[0030] (4) When the height difference between the overflow weir and the overflow outlet of the water bath is 450 mm, the liquid foam splash height in the device reaches 500 mm, exceeding the height of the overflow weir plate by 50 mm. The overflow water flows back into the overflow weir from the same part at the lower part of the overflow weir to form a stable and continuous circulating water; after calculation, the heat transfer coefficient of the water bath is consistent with the theoretical value. The theoretical temperature of the medium in the heat exchange tube should be -5°C, and the experimental value is -5°C, and the SCV works well.

[0031] (5) When the height difference between the overflow weir and the overflow outlet of the water bath is 500 mm, the liquid foam splash height in the device reaches 460 mm, exceeding the height of the overflow weir plate by 10 mm. The overflow water flows back into the overflow weir from the same part at the lower part of the overflow weir to form a partially continuous circulating water; after calculation, the heat transfer coefficient of the water bath is consistent with the theoretical value. The theoretical temperature of the medium in the heat exchange tube should be -5°C, and the experimental value is -4°C, and the SCV can operate normally.

[0032] The above experimental data can show that: First, at a suitable initial liquid level, effective overflow should be formed at the cofferdam after bubbling, and the overflow water flows back into the overflow weir from the same part at the lower part of the overflow weir to form intense circulating water, so that the gas-liquid two-phase flow always scours the tube bundle wall at a high speed, strengthening the heat transfer capacity in the SCV water bath; Second, the height difference can be 450 ± 50 mm as the effective initial liquid level and can be selected within this range. It can not only form effective circulating disturbance but also prevent the liquid level in the water bath from bubbling violently, ensuring that the SCV can work normally and stably, and improving the heat transfer coefficient outside the tube.

[0033] In an exemplary embodiment, the main blower is used to supply pressurized air and fuel gas to burn in the combustion chamber to generate flue gas. The pressurized air provided by the main blower 5 and the fuel gas burn in the burner 9 to generate flue gas. The combustion system always maintains a large amount of air. This appropriate air excess coefficient ensures an increase in the flue gas volume, an increase in the agitation of the water bath, and a certain degree of strengthening of heat transfer, guaranteeing the heat exchange efficiency in the water bath.

[0034] In an exemplary embodiment, the flue gas enters the flue gas bubbler 6 through the combustion chamber 8. The distance between the bottom of the flue gas bubbler 6 and the bottom of the water bath ranges from 190 to 210 mm. Determining the distance within the range of 190 to 210 mm can make the amount of bubbles contained in the water bath as large as possible, increasing the heat transfer area between the gas and the liquid, thereby ensuring the stability of the heat transfer turbulence above the tube bundle.

[0035] The experimental data shows that:

[0036] (1) When the distance between the bottom of the flue gas bubbler 6 and the bottom of the water bath is 180 mm, the immersion depth is relatively deep, the amount of bubbles contained in the water bath is relatively large, the heat transfer coefficient of the water bath does not match the theoretical value well, and the theoretical temperature of the medium in the heat exchange tube should be -5 °C, while the experimental value is only -8 °C;

[0037] (2) When the distance between the bottom of the flue gas bubbler 6 and the bottom of the water bath is 220 mm, the immersion depth is relatively shallow, the amount of bubbles contained in the water bath is relatively small, the effective disturbance is relatively low, the heat transfer coefficient of the water bath does not match the theoretical value well, and the theoretical temperature of the medium in the heat exchange tube should be -5 °C, while the experimental value is only -8 °C;

[0038] (3) When the distance between the bottom of the flue gas bubbler 6 and the bottom of the water bath is 200 mm, the appropriate immersion depth makes the amount of bubbles contained in the water bath as large as possible, with effective disturbance, thus ensuring the stability of the heat transfer turbulence above the tube bundle. The heat transfer coefficient of the water bath matches the theoretical value, and the theoretical temperature of the medium in the heat exchange tube should be -5 °C, and the experimental value is also -5 °C.

[0039] In an exemplary embodiment, the flue gas enters the water in the water bath through a number of openings 7 in the upper part of the flue gas bubbler 6. The opening ratio of the flue gas bubbler ranges from 0.009 ± 0.001, and the flue gas outlet velocity ranges from 40 ± 2 m / s. This appropriate opening ratio causes the flue gas outlet velocity to increase, forming a local and intense agitation of the water bath, increasing the gas holdup in the overflow weir, and enabling the improvement of the heat transfer coefficient outside the tube. A lower opening ratio causes the flue gas outlet velocity to increase, forming a local and intense agitation of the water bath, increasing the liquid phase volume overflowing outside the overflow weir, with a relatively high gas holdup in the overflow weir, resulting in a relatively low heat transfer coefficient outside the tube.

[0040] According to the test data, when the opening ratio of the flue gas bubbler is 0.007, the gas holdup in the overflow weir is relatively low, resulting in a relatively low heat transfer coefficient outside the tube.

[0041] When the opening ratio of the flue gas bubbler is 0.011, the excessive gas holdup causes a sharp increase in the gas holdup in the water bath, leading to a deterioration of heat transfer in the shell side.

[0042] According to the test data, when the flue gas outlet velocity is 36 m / s, it cannot form a good disturbance to the water bath, the gas holdup in the overflow weir is inappropriate, and the water level rise is small, resulting in the inability of the water bath to overflow to form circulating water. The heat transfer coefficient of the water bath does not match the theoretical value well. The theoretical temperature of the medium in the heat exchange tube should be -5 °C, and the experimental value is only -21 °C;

[0043] According to the test data, when the flue gas outlet velocity is 43 m / s, it leads to an excessive gas holdup, causing a sharp increase in the gas holdup in the water bath, resulting in a deterioration of heat transfer in the shell side. The heat transfer coefficient of the water bath does not match the theoretical value well. The theoretical temperature of the medium in the heat exchange tube should be -5 °C, and the experimental value is only -10 °C;

[0044] According to the test data, when the flue gas outlet velocity is 38 m / s, it has a good disturbance to the water bath, the gas holdup in the overflow weir is appropriate, the heat transfer effect in the shell side is good, the heat transfer coefficient of the water bath is relatively consistent with the theoretical value, the theoretical temperature of the medium in the heat exchange tube should be -5 °C, and the experimental value is -6 °C;

[0045] According to the test data, when the flue gas outlet velocity is 42 m / s, it has a good disturbance to the water bath, the gas holdup in the overflow weir is appropriate, the heat transfer effect in the shell side is good, the heat transfer coefficient of the water bath is relatively consistent with the theoretical value, the theoretical temperature of the medium in the heat exchange tube should be -5 °C, and the experimental value is -6 °C.

[0046] Based on the above analysis, it is obtained that:

[0047] (1) Determine this opening ratio and flow velocity according to the test. The appropriate opening ratio ensures an appropriate gas holdup in the overflow weir and the stability of the heat transfer turbulence above the tube bundle, enabling the shell side heat transfer efficiency of the device to reach a relatively high level and effectively reducing the equipment vibration caused by the water flow fluctuation resonance.

[0048] (2) The height difference of 450 mm between the overflow weir and the overflow opening of the water bath is used as the initial liquid level, the opening ratio of the flue gas bubbler is determined to be 0.009, and the distance between the bottom of the air bubbler and the bottom of the water bath is 200 mm. These three can vary independently within a certain range but are interrelated.

[0049] (3) It has been experimentally proven that the combination of these three values is the best match, which can form a vigorous water circulation and a suitable gas holdup within the overflow weir, ensuring enhanced heat transfer capacity, a stable turbulent flow for heat exchange above the tube bundle, and effective reduction of equipment vibration.

[0050] In an exemplary embodiment, the heat exchange coil 4 is immersed in the water of the water bath 1. By exchanging heat with the strongly bubbling water, the LNG at the inlet of the heat exchange coil 4 is vaporized into NG at the outlet of the heat exchange coil 4. The flow rate of the LNG at the tube side inlet is determined to be between 0.8 and 3 m / S. This appropriate flow rate inside the tube ensures a relatively high heat transfer coefficient on the tube side, resulting in a smaller heat exchange area and reduced initial investment.

[0051] Example 1

[0052] A heat exchange system of a new type of submerged combustion vaporizer, as Figure 1 shown, includes: a water bath 1, an overflow opening 2, an overflow weir 3, a heat exchange coil 4, a main fan 5, a flue gas bubbler 6, upper openings 7 of the bubbler, and a combustion chamber 8.

[0053] Among them: A certain amount of water is contained in the water bath 1 up to a certain liquid level line. The water bath 1 is provided with an overflow opening 2. The height difference of 450 mm between the overflow weir 3 and the overflow opening 2 of the water bath is used as the initial liquid level. Part of the combustion chamber 8, part of the overflow weir 3, all of the flue gas bubbler 6, and all of the heat exchange coil 4 are immersed in water. There is a distance of 200 mm between the bottom of the flue gas bubbler 6 and the bottom of the water bath. A number of openings 7 are provided in the upper part of the flue gas bubbler 6.

[0054] Example 2

[0055] The present invention provides a heat exchange system of a new type of submerged combustion vaporizer. The heat exchange process achieved includes the following steps:

[0056] Step 1, the pressurized air provided by the main fan 5 and the fuel gas burn in the burner 9 to generate flue gas. The combustion system always maintains a relatively large amount of air. This appropriate air excess coefficient ensures an increase in the amount of flue gas, an increase in the agitation of the water bath, and a certain degree of heat transfer enhancement, guaranteeing the heat exchange efficiency within the water bath.

[0057] Step 2: The flue gas enters the flue gas bubbler 6 through the combustion chamber 8. The distance between the bottom of the flue gas bubbler 6 and the bottom of the water bath is determined to be 200 mm. This appropriate immersion depth enables the water bath to contain as many bubbles as possible, increasing the heat transfer area between the gas and liquid, and thus ensuring the stability of the heat transfer turbulence above the tube bundle.

[0058] Step 3: The flue gas enters the water in the water bath through several openings 7 in the upper part of the flue gas bubbler 6. The opening ratio of the flue gas bubbler is determined to be 0.009, and the flue gas outlet velocity is determined to be 40 m / s. This appropriate opening ratio causes the flue gas outlet velocity to increase, forming a local and intense agitation of the water bath, increasing the gas holdup in the overflow weir, and improving the heat transfer coefficient outside the tubes.

[0059] Step 4: The height difference of 450 mm between the overflow weir 3 and the overflow opening 2 of the water bath is used as the initial liquid level. This appropriate initial liquid level can not only form an effective circulation disturbance but also prevent the liquid level in the water bath from bubbling violently, ensuring the normal operation and stable operation of the SCV and improving the heat transfer coefficient outside the tubes.

[0060] Step 5: The heat exchange coil 4 is immersed in the water in the water bath 1. By exchanging heat with the strongly bubbling water, the LNG at the inlet of the heat exchange coil 4 is vaporized into NG at the outlet of the heat exchange coil 4. The flow rate of the LNG at the tube side inlet is determined to be between 0.8 and 3 m / s. This appropriate flow rate inside the tube ensures a relatively high heat transfer coefficient in the tube side, resulting in a smaller heat transfer area and a reduced one-time investment.

[0061] The above example has the following technical effects:

[0062] 1. When the flow rate of the LNG at the tube side inlet is increased to between 0.8 and 3 m / s, the heat transfer coefficient in the tube side is relatively high, the heat transfer area is smaller, and the one-time investment is reduced.

[0063] 2. Optimize the initial liquid level height, that is, the height difference between the overflow weir and the overflow opening of the water bath, to ensure the formation of an effective circulation disturbance and the normal operation and stable operation of the SCV.

[0064] 3. Through the main fan, the upstream combustion system is always maintained with a large amount of air, the air excess coefficient is large, the flue gas volume increases, and the heat transfer is strengthened to a certain extent, ensuring the heat exchange efficiency in the water bath.

[0065] 4. Determine the optimal immersion depth of the flue gas bubbler; since it determines the residence time of the flue gas in the water bath, an appropriate immersion depth can make the water bath contain as many bubbles as possible, increasing the heat transfer area between the gas and liquid, and thus ensuring the stability of the heat transfer turbulence above the tube bundle.

[0066] 5. Determine the optimal porosity of the flue gas bubbler, so that the flue gas outlet velocity increases, forming a local and intense agitation of the water bath, increasing the gas holdup in the overflow weir, and improving the heat transfer coefficient outside the tube.

[0067] Those of ordinary skill in the art can understand that all or some of the steps in the methods disclosed above, and the functional modules / units in the systems and devices, can be implemented as software, firmware, hardware, and their appropriate combinations. In the hardware implementation, the division between the functional modules / units mentioned above does not necessarily correspond to the division of physical components; for example, one physical component may have multiple functions, or one function or step may be executed by several physical components in cooperation. Some or all of the components may be implemented as software executed by a processor, such as a digital signal processor or a microprocessor, or may be implemented as hardware, or may be implemented as an integrated circuit, such as an application-specific integrated circuit. Such software can be distributed on a computer-readable medium, which may include a computer storage medium (or non-transitory medium) and a communication medium (or transitory medium). As is well known to those of ordinary skill in the art, the term computer storage medium includes volatile and non-volatile, removable and non-removable media implemented in any method or technology for storing information, such as computer-readable instructions, data structures, program modules, or other data. Computer storage media include, but are not limited to, RAM, ROM, EEPROM, flash memory or other memory technologies, CD-ROM, digital versatile disk (DVD) or other optical disk storage, magnetic cassette, tape, magnetic disk storage or other magnetic storage devices, or any other medium that can be used to store the desired information and can be accessed by a computer. In addition, as is well known to those of ordinary skill in the art, a communication medium typically contains computer-readable instructions, data structures, program modules, or other data in a modulated data signal such as a carrier wave or other transmission mechanism, and may include any information delivery medium.

Claims

1. A heat exchange system of a submerged combustion gasifier, characterized in that, The system includes: a water bath, an overflow port, an overflow weir, and a flue gas bubbler; Wherein, the overflow port is provided on the water bath, and the height difference between the overflow weir and the overflow port ranges from 400 to 500 mm; The distance between the bottom of the flue gas bubbler and the bottom of the water bath ranges from 190 to 210 mm.

2. The heat exchange system of the submerged combustion gasifier according to claim 1, wherein, The system further includes: a main blower, a heat exchange coil, and a combustion chamber.

3. The heat exchange system of the submerged combustion gasifier according to claim 1, wherein, The height difference between the overflow weir and the overflow port is 400 mm or 410 mm or 420 mm or 430 mm or 440 mm or 450 mm or 460 mm or 470 mm or 480 mm or 490 mm or 500 mm.

4. The heat exchange system of the submerged combustion gasifier according to claim 3, wherein, The height of the overflow port is used as the initial liquid level.

5. The heat exchange system of the submerged combustion gasifier according to claim 1, wherein The distance between the bottom of the flue gas bubbler and the bottom of the water bath is 190 mm or 195 mm or 200 mm or 205 mm or 210 mm.

6. The heat exchange system of the submerged combustion gasifier according to claim 2, wherein, The main blower is used to provide pressurized air and fuel gas to burn in the combustion chamber to generate flue gas.

7. The heat exchange system of the submerged combustion gasifier according to claim 1, wherein, Multiple openings are provided in the upper part of the flue gas bubbler; Wherein, the opening ratio of the flue gas bubbler ranges from 0.008 to 0.010, and the flue gas outlet velocity ranges from 38 to 42 m / s.

8. The heat exchange system of the submerged combustion gasifier according to claim 7, wherein, The opening ratio of the flue gas bubbler is 0.008 or 0.009 or 0.010; The flue gas outlet velocity is 38 m / s or 39 m / s or 40 m / s or 41 m / s or 42 m / s.

9. The heat exchange system of the submerged combustion gasifier according to claim 2, wherein, The heat exchange coil is submerged in the water bath and is used to exchange heat with the bubbling water to vaporize the imported LNG into the exported NG.

10. The heat exchange system of the submerged combustion gasifier according to claim 7, characterized in that, The heat exchange coil is further used to set the flow velocity of the LNG at the inlet of the tube side to 0.8 to 3 m / s.

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