CN114272714A - Benzene vapor condensation cooling system of debenzolization tower by using air cooler - Google Patents
Benzene vapor condensation cooling system of debenzolization tower by using air cooler Download PDFInfo
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- CN114272714A CN114272714A CN202111642932.2A CN202111642932A CN114272714A CN 114272714 A CN114272714 A CN 114272714A CN 202111642932 A CN202111642932 A CN 202111642932A CN 114272714 A CN114272714 A CN 114272714A
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Abstract
The invention belongs to the technical field of benzene vapor condensation cooling of a debenzolization tower, and particularly relates to a benzene vapor condensation cooling system of the debenzolization tower by using an air cooler, which comprises a first-section air cooler, a gas-liquid separator and a second-section air cooler, wherein one end of the first-section air cooler is communicated with a benzene vapor outlet of the debenzolization tower, the other end of the first-section air cooler is communicated with an inlet of the gas-liquid separator, and an air outlet of the gas-liquid separator is communicated with an air inlet of the second-section air cooler; the invention utilizes the renewable resource of nature air to replace circulating cooling water of an open cooling tower to condense, cool and reduce the temperature of high-temperature benzene steam produced by the debenzolization tower, is a revolutionary technical change and subversive innovation in the professional aspect of benzene steam condensation and cooling of the debenzolization tower, has the advantages of energy conservation, environmental protection, safety and simple and convenient operation, belongs to clean and environment-friendly production, develops a more energy-saving, more environment-friendly, lower cost, simpler and safer production process device, and has good optimization effect on various operation indexes of the debenzolization tower.
Description
Technical Field
The invention belongs to the technical field of benzene vapor condensation and cooling of a debenzolization tower, and particularly relates to a benzene vapor condensation and cooling system of the debenzolization tower by using an air cooler.
Background
As shown in fig. 1, in the conventional process, benzene vapor generated after the treatment of a debenzolization tower a is condensed by a crude condensation cooler b and a benzene vapor cooler d, and is separated by a vapor-liquid separator c, and is cooled by an open-circuit cooling tower circulating cooling water system e, cooling water is introduced into a circulating cooling water reservoir f, and circulating water then flows back to a heat exchange system g, and the system has the following disadvantages:
1. the traditional process adopts an open-circuit cooling tower circulating cooling water system, and because of evaporation loss of cooling tower water and the objective existence of frequent pollution discharge for ensuring water quality, the consumption index of fresh water per ton of coke is high, and the energy consumption of unit procedure is difficult to control below a unit product energy consumption limit admission value 122 kgce/ton coke of a newly-built coke production device in a coke unit product energy consumption limit (GB 21342-2013); with the required quantity of circulating cooling water 4400m3Calculated by/h, the amount of water resources wasted per hour is specifically as follows: the evaporation loss is 82.94m3H, the loss of wind-blown splash is 4.4m3Per h, the pollution discharge loss is 39m3/h。
The total reserve of water on the earth is about 13.9 x 108Km3And about 97 percent of the salt water is ocean salt water which cannot be directly utilized by human beings. The total amount of fresh water is only 0.36 × 108Km3And 77.2% of fresh water which is less than 3% of the total water of the earth exists on polar regions and mountains in the form of glaciers and ice caps, and is difficult to be directly utilized by human; 22.4% is groundwater and soil water, wherein 2/3 groundwater is deeply buried in the ground; the total amount of ground water of rivers, lakes and the like is only 0.36 percent of the total amount of fresh water. Only 20% of the fresh water is easy to be used by human beings, and the fresh water of rivers and lakes which can be directly taken and used only accounts for 0.3% of the total amount of the fresh water, so that the fresh water resource for the direct use of the human beings is very limited.
2. The circulating water is added with agents such as a sterilization algicide and a scale and corrosion inhibitor (with corrosivity) every day, the annual agent cost is 21-22 ten thousand yuan, the operation cost and the labor intensity of workers are increased, the environment is polluted, and the method is not energy-saving and environment-friendly.
3. The heat exchange tube array circulating cooling water channels of the crude benzene condensation cooler and the benzene vapor cooler are easy to scale, chemical cleaning is needed once every year, equipment accidents such as internal leakage and the like of the crude benzene condensation cooler and the benzene vapor cooler are caused by frequent cleaning, and the service life of the equipment is shortened.
4. After the heat exchange tube array circulating cooling water channels of the crude benzene condensation cooler and the benzene gas cooler are scaled, waste liquid generated in the chemical cleaning process belongs to hazardous waste and is not easy to treat.
Therefore, there is a need for an improved benzene vapor condensation cooling system for the above-mentioned debenzolization column.
Disclosure of Invention
In order to solve the technical problem, the invention provides a benzene vapor condensation cooling system of a debenzolization tower by using an air cooler.
The invention is realized by the following technical scheme.
A benzene vapor condensation cooling system of a debenzolization tower by utilizing an air cooler comprises a first-section air cooler, a gas-liquid separator and a second-section air cooler, wherein one end of the first-section air cooler is communicated with a benzene vapor outlet of the debenzolization tower, the other end of the first-section air cooler is communicated with an inlet of the gas-liquid separator, and an air outlet of the gas-liquid separator is communicated with an air inlet of the second-section air cooler;
the one section of air cooler and the two-section air cooler are identical in structure and respectively comprise two groups of heat exchange tubes and a draught fan, the two groups of heat exchange tubes are arranged in a V shape, the draught fan is arranged above the heat exchange tubes of the V shape, and benzene steam is guided away from a tube pass and indirectly exchanges heat with air outside the heat exchange tubes.
Preferably, the heat exchange tube nest is a tube body composed of a base layer and a coating layer, the base layer is made of carbon steel, the coating layer is made of stainless steel 304, fins are arranged on the outer wall of the heat exchange tube nest, and the fins are made of 1060 Al.
Preferably, the first stage air cooler and the second stage air cooler are respectively provided with a set of low pressure compressed air cleaning system, and the low pressure compressed air cleaning system includes: the heat exchange device comprises a bottom frame and an installation pipe, wherein the bottom frame is arranged above the V-shaped heat exchange array pipe, the installation pipe is fixedly connected to the bottom frame vertically, three compressed air nozzles are uniformly distributed on the installation pipe from top to bottom, and the compressed air nozzles and a compressed air main pipe of an air compression station are connected through a pressure-resistant hose and a quick coupling.
Preferably, after the heat exchange between the air outside the heat exchange tube array and the benzene steam in the tube, the induced draft fan continuously exhausts the air, and the fan rotating speed is controlled by adjusting the frequency of the induced draft fan to control the temperature of the benzene steam mixed gas cooler in the tube.
Preferably, the temperature of the benzene steam at the outlet of the debenzolization tower is 80-90 ℃, and the mixture of the benzene steam and benzene is formed after passing through the first-section air cooler, and the temperature is 25-30 ℃.
Preferably, the temperature of the uncondensed benzene steam after separation by the gas-liquid separator is 25-30 ℃.
Preferably, after condensation by the two-stage air cooler, uncondensed steam is pumped to a gas pipeline in front of the benzene washing tower by a vacuum unit for tail gas recovery, and condensed benzene flows to the gas-liquid separator for separation.
Preferably, the liquid phase in the gas-liquid separator directly flows to a crude benzene oil-water separator by utilizing the potential difference to perform oil-water separation, crude benzene separated by the crude benzene oil-water separator enters a crude benzene reflux tank, part of the crude benzene is sent to the top of a debenzolization tower by a crude benzene reflux pump to be refluxed, the rest of the crude benzene enters a crude benzene intermediate tank, the crude benzene is sent to an oil depot tank area for sale by a crude benzene delivery pump after being metered, and the water phase separated by the crude benzene oil-water separator flows to a control separator.
Compared with the prior art, the invention has the following beneficial effects:
the invention improves the traditional benzene vapor condensation cooling system of the debenzolization tower, utilizes renewable resources of nature air to replace circulating cooling water of an open-circuit cooling tower to condense, cool and cool high-temperature benzene vapor produced by the debenzolization tower, can condense, cool and cool 80-90 ℃ benzene vapor (containing water vapor) evaporated from a semi-negative pressure debenzolization tower to 25-30 ℃, and has the following advantages compared with the traditional process system for condensing, cooling and cooling the benzene vapor by using the circulating cooling water system of the open-circuit cooling tower, a crude benzene condensation cooler and a benzene vapor cooler:
(1) and no circulating water pump is arranged, so that the power consumption is reduced.
(2) Fresh water is not consumed any more by the system, the fresh water consumption per ton of coke is reduced, and the energy consumption per unit procedure is better controlled to be below a unit product energy consumption allowance admission value of 122kgce/t coke of a newly built coke production device in the coke unit product energy consumption allowance (GB 21342-2013).
(3) The air of nature is used as cooling medium, so that the environment is protected.
(4) The system does not need to add a sterilization algicide and a scale and corrosion inhibitor (with corrosivity), does not have the phenomenon that pipeline scaling needs frequent chemical cleaning, prolongs the service life of equipment, reduces the operation cost, is environment-friendly, safe and simple to operate, and does not generate hazardous wastes.
The device is revolutionary technical change and subversive innovation in the benzene steam condensation cooling professional aspect of the debenzolization tower, has the advantages of energy conservation, environmental protection, safety and simple and convenient operation, belongs to clean and environment-friendly production, develops a production process device with more energy conservation, more environmental protection, lower cost, simpler and safer operation indexes, and has good optimization effect on the benzene removal tower.
Drawings
FIG. 1 is a benzene vapor condensing and cooling system of a conventional debenzolization tower;
FIG. 2 is a benzene vapor condensing and cooling system of a debenzolization tower using an air cooler provided by the present invention;
FIG. 3 is a schematic diagram of a specific structure of the primary air cooler or the secondary air cooler in FIG. 2;
description of reference numerals:
a. b, a debenzolization tower, a crude benzene condensation cooler, c, a vapor-liquid separator, d, a benzene vapor cooler, e, an open-circuit cooling tower circulating cooling water system, f, a circulating cooling water reservoir, g, a heat exchange system, h and a rich oil heater;
1. the device comprises a first-section air cooler, a second-section air cooler, a heat exchange tube array, a draught fan, a base frame, a compressed air nozzle and an installation tube, wherein the first-section air cooler is 2, the second-section air cooler is 3, the heat exchange tube array is 4, the draught fan is 5, the base frame is 51, and the installation tube is 52.
Detailed Description
In order to make the technical solutions of the present invention better understood and implemented by those skilled in the art, the present invention is further described below with reference to the following specific embodiments and the accompanying drawings, but the embodiments are not meant to limit the present invention. The experimental methods and the detection methods described in the following examples are all conventional methods unless otherwise specified; the reagents and materials are commercially available, unless otherwise specified.
4 JNX2-70-2 model single-heating top-loading coke oven producing 280 ten thousand tons of coke annually, gas purifying device matched with the top-loading coke oven and implemented in two stages, and gas treatment capacity (dry gas) of 77602Nm3H multiplied by 2, purified coke oven gas for industrial or civil use. The benzene content of the coke oven gas before purification is 22-24 g/m3Cooling the coal gas from the ammonium sulfate unit in a direct final cooling tower, cooling the coal gas to 25-27 ℃, then passing the cooled coal gas through a mist catcher to catch water mist droplets carried in the coal gas, then feeding the coal gas into a benzene washing tower from bottom to top, and spraying the coal gas at 27-28 ℃ and 300m at the top of the benzene washing tower3The/h wash oil is in reverse contact, and the gas is subjected to benzene washing purification and then contains benzene to not more than 0.5g/Nm3Sending the coal gas to a subsequent use unit, enabling the washing oil to absorb the benzene hydrocarbon in the coal gas to become rich oil containing 2.1-2.5% of benzene, pressurizing the rich oil by a rich oil pump, performing heat exchange with the lean oil through a first-stage lean rich oil heat exchanger and a second-stage lean rich oil heat exchanger, controlling the temperature to be-150 ℃, then indirectly heating the rich oil by using medium-pressure steam with the pressure of 3.6MPa and the temperature of 390 ℃ to 170-180 ℃ through a rich oil heater h (shown in figure 1), then enabling the rich oil to enter the middle-lower part of a debenzolization tower a for debenzolization and stripping and rectification to produce crude benzene, introducing 350-390 ℃ to the lower part of the debenzolization tower a, controlling the top pressure of the semi-negative pressure debenzolization tower to be-30 KPa, and controlling the temperature of the top of the debenzolization tower to be 80-90 ℃.
As shown in fig. 1, in the conventional process, benzene vapor in a debenzolization tower is cooled by adopting an open-circuit cooling tower circulating cooling water, a crude benzene condensation cooler and a benzene vapor cooler, which wastes water resources, wastes electric energy and is difficult to clean, and chemical reagents are required to be used, so that the process is not beneficial to long-term use of equipment, and the like, therefore, the invention provides a debenzolization tower benzene vapor condensation cooling system using an air cooler, which comprises a first-section air cooler 1, a gas-liquid separator c and a second-section air cooler 2 as shown in fig. 2, wherein one end of the first-section air cooler 1 is communicated with a benzene vapor outlet of a debenzolization tower a, the other end of the first-section air cooler is communicated with an inlet of the gas-liquid separator c, and an air outlet of the gas-liquid separator c is communicated with an air inlet of the second-section air cooler 2; one section air cooler 1 with 2 structures of two-stage segment air cooler are the same, all include two sets of heat transfer tubulation 3 and draught fan 4, and are two sets of heat transfer tubulation 3 become the V type and arrange, draught fan 4 sets up in the heat transfer tubulation 3 top of V type, benzene gas walk the tube side and with the indirect heat transfer is carried out to 3 outside of tubes of heat transfer tubulation air. It should be noted here that the structural style of the air condensing cooler is a "V-type induced draft" structure, and a type a air cooling condenser of a power plant cannot be used, because the collection, collection and drainage of the condensed benzene-water mixture are facilitated. 3 outside of tubes's of heat transfer tubulation air and intraductal benzene steam heat exchange back, pass through in draught fan 4 continuously arranges to the atmosphere, and through adjusting draught fan 4 frequency control fan rotational speed, control intraductal benzene gas mixture gas cooler rear temperature. The cooling method comprises the following steps: benzene steam is led to in the intraductal benzene that leads to of heat transfer tubulation 3, and the outside of tubes contacts with outside air, and the air temperature outside the tubes is low, and the heat of benzene steam is absorbed by the air, and draught fan 4 constantly arranges the outside air of heat transfer tubulation 3 to the atmosphere in, reduces the temperature of near air outside heat transfer tubulation 3 for the heat of benzene steam can continuously be absorbed, thereby has realized the refrigerated purpose of condensation. In addition, the rotating speed of the draught fan can be controlled by adjusting the frequency of the draught fan 4, and the air quantity is indirectly controlled, so that the temperature of the benzene-gas mixture cooler in the pipe is controlled.
The benzene has corrosivity, so that the pipeline can be corroded after long-time use, in order to prevent the problem, the pipeline is prepared by using an anticorrosive material, specifically, the pipeline is prepared by using a stainless steel composite plate which is formed by combining carbon steel serving as a base layer and stainless steel 304 serving as a coating layer, the base layer and the coating layer are completely metallurgically combined, the composite material is a novel material, the complementary advantages of the material are fully realized, the corrosion resistance, the wear resistance, the diamagnetism and the decoration of 304 are realized, the composite material also has good weldability, the formability, the ductility and the heat conductivity of the carbon steel, the strength, the rigidity and the impact load strength can be obviously improved by using the composite material, the weight of a structural member is reduced, the cost can be greatly reduced while the technical requirements are ensured, and the composite material is a new-generation energy-saving and environment-friendly product. The outer diameter of the tube array is 25mm, the wall thickness is 3mm, the material of fins on the outer wall of the tube array is 1060Al, the height of the fins is 16mm, the thickness of the fins is 0.4m, the fin ratio is 23.4, the fin type DR is adopted, and the tube drainage is a 4-row 2 process. The head-on wind speed is 2.8 m/s. The number of the tube bundles is 24, and the number of the single-tube-bundle heat exchange tubes is 200.
The temperature of benzene steam at the outlet of the debenzolization tower a is 80-90 ℃, and after passing through the first-section air cooler 1, a mixture of the benzene steam and benzene is formed, and the temperature is 25-30 ℃. The rotating speed of the draught fan is controlled by adjusting the frequency of the draught fan, the cooling air quantity is indirectly controlled, the temperature of the benzene-water mixture is controlled, the temperature cannot be lower than 20 ℃, and the condition that the condensed benzene-water mixture enters the oil-water separator in winter and is frozen to damage an equipment pipeline due to low external temperature is avoided. The temperature of the benzene gas separated by the gas-liquid separator is 25-30 ℃, and the benzene gas automatically flows into a two-stage air cooler to be condensed and then is cooled to about 25 ℃ through indirect heat exchange with air. The rotating speed of the draught fan is controlled by adjusting the frequency of the draught fan, the cooling air quantity is indirectly controlled, the temperature of the benzene-water mixture is controlled, the temperature cannot be lower than 20 ℃, and the condition that the condensed benzene-water mixture enters the oil-water separator in winter and is frozen to damage an equipment pipeline due to low external temperature is avoided.
The first stage air cooler 1 and the second stage air cooler 2 are respectively provided with a set of low pressure compressed air cleaning system, as shown in fig. 3, the low pressure compressed air cleaning system includes: the heat exchange device comprises a bottom frame 5 and installation pipes 52, wherein the bottom frame 5 is arranged above the V-shaped heat exchange tubes 3, the installation pipes 52 are fixedly connected to the bottom frame 5 vertically, three compressed air nozzles 51 are uniformly distributed on the installation pipes 52 from top to bottom, and the compressed air nozzles 51 are connected with compressed air main pipes of an air compression station through pressure-resistant hoses and quick joints. Compressed air source parameters: air quantity is 500m3The compressed air pressure requirement is 0.15MPa (g). The traditional process needs to regularly carry out chemical cleaning on a crude benzene condensation cooler, a benzene vapor cooler and the like due to frequent chemical cleaningThe low-pressure compressed air cleaning system does not need to be washed by clear water any more, makes full use of redundant compressed air in a plant area, saves water resources, avoids the current situation of corrosion of the outer wall of the equipment tube when the equipment tube is washed by water, and is energy-saving and environment-friendly.
Crude benzene vapor evaporated from the tower top of the debenzolization tower a enters a first-stage air cooler 1, is condensed and cooled to 25-30 ℃ by natural air to form a gas-liquid mixture, then enters a horizontal gas-liquid separator for gas-liquid separation, a liquid phase in the gas-liquid separator c directly flows to a crude benzene oil-water separator for oil-water separation by utilizing the potential difference of the liquid phase, a gas phase part enters a second-stage air cooler 2 for secondary condensation and cooling, uncondensed benzene vapor is pumped to a gas pipeline in front of a benzene washing tower by a vacuum unit for tail gas recovery, and the vacuum degree of the debenzolization tower is strictly controlled and adjusted to be kept at-30 KPa. And the condensed benzene flows to the gas-liquid separator c for separation, the crude benzene separated by the crude benzene oil-water separator enters a crude benzene reflux groove, part of the crude benzene is sent to the top of the debenzolization tower through a crude benzene reflux pump to be refluxed, and the rest of the crude benzene enters a crude benzene intermediate groove. The crude benzene is sent to the oil depot tank area for sale by a crude benzene delivery pump after being metered. The water phase separated from the crude benzene oil-water separator automatically flows to the control separator.
The invention improves the traditional benzene vapor condensation cooling system of the debenzolization tower, utilizes renewable resources such as nature air to replace circulating cooling water of an open-circuit cooling tower to condense, cool and cool high-temperature benzene vapor produced by the debenzolization tower, can condense, cool and cool 80-90 ℃ benzene vapor (containing water vapor) evaporated by a semi-negative pressure debenzolization tower to 25-30 ℃, does not consume fresh water in the system, reduces the consumption of fresh water per ton of coke, and better controls the energy consumption of unit procedure to be below the unit product energy consumption allowance admittance value of a newly-built coke production device in the coke unit product energy allowance (GB21342-2013) of 122kgce/t coke. The air of nature is used as cooling medium, so that the environment is protected. The system does not need to add a sterilization algicide and a scale and corrosion inhibitor (with corrosivity), does not have the phenomenon that the pipeline is scaled and needs frequent chemical cleaning, and prolongs the service life of equipment. The method has the advantages of low operation cost, environmental protection, safety, simple operation and no generation of hazardous wastes. The device is revolutionary technical change and subversive innovation in the benzene steam condensation cooling professional aspect of the debenzolization tower, has the advantages of energy conservation, environmental protection, safety and simple and convenient operation, belongs to clean and environment-friendly production, develops a production process device with more energy conservation, more environmental protection, lower cost, simpler and safer operation indexes, and has good optimization effect on the benzene removal tower.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, it is intended that such changes and modifications be included within the scope of the appended claims and their equivalents.
Claims (8)
1. The benzene vapor condensation cooling system for the debenzolization tower by using the air cooler is characterized by comprising a first-stage air cooler (1), a gas-liquid separator (c) and a second-stage air cooler (2), wherein one end of the first-stage air cooler (1) is communicated with a benzene vapor outlet of the debenzolization tower (a), the other end of the first-stage air cooler is communicated with an inlet of the gas-liquid separator (c), and a vapor outlet of the gas-liquid separator (c) is communicated with a vapor inlet of the second-stage air cooler (2);
one section air cooler (1) with two-section air cooler (2) structure is the same, all includes two sets of heat transfer tubulation (3) and draught fan (4), and is two sets of heat transfer tubulation (3) become the V type and arrange, draught fan (4) set up in the heat transfer tubulation (3) top of V type, benzene steam walk the tube side and with the air of heat transfer tubulation (3) outside of the tubes carries out indirect heat transfer.
2. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein the heat exchange tubes (3) are tubes composed of a base layer and a coating layer, the base layer is made of carbon steel, the coating layer is made of stainless steel 304, the outer walls of the heat exchange tubes are provided with fins, and the fins are made of 1060 Al.
3. The benzene vapor condensation cooling system of the debenzolization tower using an air cooler as claimed in claim 1, wherein said primary air cooler (1) and said secondary air cooler (2) are respectively equipped with a set of low pressure compressed air cleaning system, said low pressure compressed air cleaning system comprising: chassis (5) and installation pipe (52), chassis (5) set up the heat transfer tubulation (3) top of V type, vertical rigid coupling has installation pipe (52) on chassis (5), installation pipe (52) top-down evenly distributed has three compressed air nozzle (51), compressed air nozzle (51) and air compression station's compressed air are responsible for between and are connected through pressure-resistant hose and quick-operation joint.
4. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein the air outside the heat exchange tubes (3) is continuously discharged to the atmosphere through the induced draft fan (4) after heat exchange with the benzene vapor inside the tubes, and the temperature of the benzene vapor mixed gas cooler inside the tubes is controlled by adjusting the frequency of the induced draft fan (4) to control the rotating speed of the fan.
5. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein the temperature of the benzene vapor at the outlet of the debenzolization tower (a) is 80-90 ℃, and after passing through the primary air cooler (1), a mixture of the benzene vapor and benzene is formed, and the temperature is 25-30 ℃.
6. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein the temperature of the uncondensed benzene vapor separated by the gas-liquid separator (c) is 25-30 ℃.
7. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein after the condensation of the second-stage air cooler (2), the benzene vapor which is not condensed is pumped to a gas pipeline before the benzene washing tower by a vacuum unit for tail gas recovery, and the condensed benzene flows to the gas-liquid separator (c) for separation.
8. The benzene vapor condensation cooling system of the debenzolization tower using the air cooler as claimed in claim 1, wherein the liquid phase in the gas-liquid separator (c) directly flows to the crude benzene oil-water separator by its own potential difference for oil-water separation, the crude benzene separated by the crude benzene oil-water separator enters the crude benzene reflux tank, part of the crude benzene is sent to the top of the debenzolization tower (a) by the crude benzene reflux pump as reflux, the rest of the crude benzene enters the crude benzene intermediate tank, the crude benzene is metered and then sent to the oil depot tank region for sale by the crude benzene delivery pump, and the water phase separated by the crude benzene oil-water separator flows to the control separator.
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