CN214881315U - Pretreatment system for deep purification of coke oven gas - Google Patents
Pretreatment system for deep purification of coke oven gas Download PDFInfo
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- CN214881315U CN214881315U CN202120350075.8U CN202120350075U CN214881315U CN 214881315 U CN214881315 U CN 214881315U CN 202120350075 U CN202120350075 U CN 202120350075U CN 214881315 U CN214881315 U CN 214881315U
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Abstract
The utility model provides a pretreatment systems of coke oven gas deep purification belongs to coke oven gas purification field to wherein impurity can cause the compressor to block up and can cause the desulfurizer of fine desulfurization to become invalid in advance and increase the problem of working costs before solving coke oven gas comprehensive utilization. The system comprises a prewashing tower, a four-phase separator, a circulating pump and a heat exchanger, wherein the prewashing tower is a supergravity rotating device, the four-phase separator is a horizontal three-weir type gas-liquid separator, and the system comprises: the gas phase inlet of the prewashing tower is connected with the coke oven gas pipeline, the liquid phase outlet of the prewashing tower is connected with the feed inlet of the four-phase separator, the intermediate phase fluid outlet of the four-phase separator is connected with the liquid inlet of the circulating pump, the liquid outlet of the circulating pump is connected with the liquid inlet of the heat exchanger, and the liquid outlet of the heat exchanger is connected with the liquid phase inlet of the prewashing tower.
Description
Technical Field
The utility model relates to a coke oven gas purifies technical field, especially relates to a coke oven gas deep purification's pretreatment systems.
Background
Coke oven gas is an important byproduct obtained in the coking process, and the research on the composition of coke oven gas has become quite mature in recent years. The coke oven gas belongs to medium-heat value natural gas, the hydrogen content is 50-60%, and the methane content is 22-24%, wherein the coke oven gas has great utilization value. A large amount of coke oven gas can be generated while producing coke, if the generation amount of the coke oven gas in China is calculated according to the condition that the coke oven gas for producing 1 ton of coke generates 430 cubic meters, the generation amount of the coke oven gas in the whole year is basically maintained at 1800 billion cubic meters, wherein about 45-50% of the coke oven gas returns to the coke oven, and the rest coke oven gas is equal to over 2 times of the gas transmission amount in the design year of 'west gas and east gas transmission' in China. Therefore, how to recycle the coke oven gas has important significance for realizing the cyclic utilization of resources and the sustainable development of economy. The purification of the coke oven gas becomes the most important thing before the coke oven gas is comprehensively utilized.
When the coke oven gas is comprehensively utilized to produce chemicals, the precision of impurities such as desulfurization, naphthalene removal and the like is insufficient, and the safe-stable-normal-full-excellent operation of a subsequent system cannot be ensured, which is mainly shown in the following three aspects:
(1) the normal operation of subsequent purification and synthesis is influenced by the over standard of sulfur and ammonia in the coke oven gas.
When the coke oven gas is used as fuel gas, the requirement is H2S is less than 500mg/Nm3Ammonia content of less than 100mg/Nm3However, the acid gas and ammonia in actual operation exceed the standards, which affects the stable operation of the system. Along with the expansion of coking scale and industrial aggregation, coke oven gas becomes important chemical raw material gas for use, and the change of the application of the coke oven gas causes that the original design index can not meet the requirement of the current use index.
(2) The coke oven gas contains tar and naphthalene, which seriously affect the normal operation of the compressor, mainly because the coke oven gas contains tar and has high naphthalene content, and the gas temperature is increased during compression to gasify and coke the tar; and naphthalene is condensed and crystallized to cause naphthalene blockage of the compressor, so that the compressor cannot normally run and is even forced to stop repairing, and the compressor is stopped for repairing only by opening for 1-2 days, so that the production is quite passive and is usually the situation of 1 opening for 2 or 1 opening for 3.
(3) The desulfurization agent of the fine desulfurization is failed in advance due to abnormal rough desulfurization, which affects the production operation, mainly sulfur penetrates, and the desulfurization agent is forced to be replaced in advance, so that the desulfurization agent is replaced frequently, and the operating cost is increased.
Disclosure of Invention
In order to solve the technical problem that impurities in the coke oven gas before comprehensive utilization can influence the stable operation of a rear system, can cause the blockage of a compressor and can cause the failure of a desulfurizing agent of fine desulfurization in advance to increase the operating cost, the utility model provides a pretreatment system for deep purification of the coke oven gas.
In order to solve the technical problem, the utility model discloses a technical scheme is:
the pretreatment system for deep purification of the coke oven gas comprises a prewashing tower, a four-phase separator, a circulating pump and a heat exchanger, wherein the prewashing tower is a supergravity rotating device, and the four-phase separator is a horizontal three-weir type gas-liquid separator, wherein: the gas phase inlet of the prewashing tower is connected with the coke oven gas pipeline after benzene elution, the liquid phase outlet of the prewashing tower is connected with the feed inlet of the four-phase separator, the intermediate phase fluid outlet of the four-phase separator is connected with the liquid inlet of the circulating pump, the liquid outlet of the circulating pump is connected with the liquid inlet of the heat exchanger, and the liquid outlet of the heat exchanger is connected with the liquid phase inlet of the prewashing tower.
Optionally, the prewashing tower comprises a transmission device, a rotating shaft and a prewashing shell, the transmission device is connected with one end of the rotating shaft, the other end of the rotating shaft is connected with a rotor, the rotor is arranged at the middle lower part of an inner cavity of the prewashing shell, a gas outlet is connected in the middle of the top of the prewashing shell, a liquid outlet is connected at the bottom of the prewashing shell, a gas inlet is connected at the bottom of one side of the prewashing shell, a liquid inlet is connected at the middle upper part of the other side of the prewashing shell, an L-shaped liquid pipeline is connected to the liquid inlet, a vertical pipe of the L-shaped liquid pipeline extends to the middle part of the rotor, a plurality of liquid nozzles are installed on the vertical pipe of the L-shaped liquid pipeline, a demister is arranged at the top of the inner cavity of the prewashing shell, a separation plate is installed between the bottom of the demister and the top of the rotor, the middle part of the top of the rotor and the separation plate are sealed by a first sealing gasket, and the middle part of the two sides of the bottom of the rotor and the rotating shaft are respectively sealed by a second sealing gasket and a third sealing gasket, the rotor is filled with a filler layer.
Optionally, the four-phase separator comprises a separation shell, and an inner cavity of the separation shell is divided into an inlet section I, a sedimentation separation section II and a collection section III from left to right; the inlet section I is provided with a gas-liquid separator, a baffle and a calming plate, the feeding hole is arranged outside the separation shell and is connected with the top of the separation shell, the gas-liquid separator is arranged below the feeding hole, the bottom end of the calming plate is connected with the bottom of the separation shell, and the top end of the baffle is connected with the top of the separation shell and is positioned between the gas-liquid separator and the calming plate; the sedimentation separation section II is provided with a coalescer; the collection section III is provided with a heavy phase fluid overflow weir, a heavy phase fluid collection groove, a light phase fluid collection groove and an intermediate phase fluid overflow weir, the heavy phase fluid overflow weir is arranged on one side of the coalescer and connected with the bottom of the separation shell, the top end of the heavy phase fluid collection groove is connected with the bottom of the separation shell and positioned between the coalescer and the heavy phase fluid overflow weir, the top and the bottom of the side wall of the heavy phase fluid collection groove are respectively provided with a first liquid level meter, the bottom of the heavy phase fluid collection groove is connected with a heavy phase fluid outlet, the top and the bottom of the separation shell above the heavy phase fluid collection groove are respectively provided with a second liquid level meter, the light phase fluid collection groove is arranged on one side of the heavy phase fluid overflow weir, the front wall of the light phase fluid collection groove is the light phase fluid overflow weir, the height of the light phase fluid overflow weir is lower than that of the rear wall of the light phase fluid collection groove, and the top and the bottom in the light phase fluid collection groove are respectively provided with a third liquid level meter, the bottom of the light phase fluid collecting tank is connected with a light phase fluid outlet, the light phase fluid outlet is positioned outside the separating shell, a demister is arranged above the light phase fluid collecting tank, the gas phase outlet is arranged outside the separating shell and connected with the demister, an intermediate phase fluid overflow weir is arranged on one side of the light phase fluid collecting tank and connected with the bottom of the separating shell, the intermediate phase fluid overflow weir and the space at the tail of the separating shell form an intermediate phase fluid collecting tank, the top and the bottom of one side of the intermediate phase fluid overflow weir are respectively provided with a fourth liquid level meter, and the bottom of the separating shell on one side of the intermediate phase fluid overflow weir is connected with an intermediate phase fluid outlet.
Optionally, the length ratio of the inlet section i, the settling separation section ii and the collection section iii is 1: 3.2-4.2: 2.
optionally, the top end of the ballast plate is at the same level with a second liquid level meter positioned at the top of the separation shell; the bottom end of the baffle is 400 mm and 500mm higher than the top end of the calming plate, and the bottom end of the baffle is not less than 200mm lower than the bottom end of the gas-liquid separator.
Optionally, the height of the coalescer is the same as the height of the light phase fluid overflow weir, the height of the heavy phase fluid overflow weir is 200-3/4 mm higher than the bottom end of the light phase fluid collection tank, the height of the light phase fluid overflow weir is 1/2-3/4 mm of the diameter of the four-phase separator, the height of the rear wall of the light phase fluid collection tank is 200mm higher than the bottom end of the demister, and the height of the intermediate phase fluid overflow weir is 20-100mm lower than the height of the light phase fluid overflow weir.
The utility model has the advantages that:
the system and the method can deeply remove harmful substances such as dust, benzene, tar, naphthalene, ammonia, sulfur and the like in the debenzolized coke oven gas, solve the problem that the standard exceeding of sulfur and ammonia in the coke oven gas can influence the stable operation of the system, and can improve the stability of the operation of the system; the problem that the compression system is blocked due to tar and naphthalene in the coke oven gas is solved, and possible blocking abnormity in the subsequent working section is avoided; the problem that the operation cost is increased due to the fact that a desulfurizing agent for fine desulfurization fails in advance due to improper rough desulfurization in the traditional process is solved, the requirements of pressurization and conveying of coke oven gas and subsequent deep purification are met, and the purpose of purifying the production chemical synthesis system is achieved. The utility model has the advantages of less investment, small equipment volume and occupied area, high efficiency of removing impurities such as tar dust, naphthalene and the like in the coke oven gas, low energy consumption, high washing efficiency and the like.
Drawings
Fig. 1 is a schematic diagram of the system of the present invention.
FIG. 2 is a schematic view of the structure of the preliminary washing column in FIG. 1.
Fig. 3 is a schematic diagram of the structure of the four-phase separator of fig. 1.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples.
As shown in fig. 1, the embodiment of the utility model provides a coke oven gas deep purification's pretreatment systems, it includes prewashing tower 1, four-phase separator 2, circulating pump 3 and heat exchanger 4, prewashing tower 1 is hypergravity rotary device, and four-phase separator 2 is horizontal three weir type gas-liquid separator, wherein: the gas phase inlet 103 of the prewashing tower 1 is connected with a coke oven gas pipeline after benzene elution, the liquid phase outlet 102 of the prewashing tower 1 is connected with the feed inlet 201 of the four-phase separator 2, the intermediate phase fluid outlet 205 of the four-phase separator 2 is connected with the liquid inlet of the circulating pump 3, the liquid outlet of the circulating pump 3 is connected with the liquid inlet of the heat exchanger 4, and the liquid outlet of the heat exchanger 4 is connected with the liquid phase inlet 109 of the prewashing tower 1.
The utility model discloses a system is used before coke oven gas deep purification (desulfurization), carries out the preliminary cooling at coke oven gas promptly, electric tar, precooling, desulfurization, intercooling, removes ammonia, carries out the preliminary treatment after final cooling and elution benzene to the impurity such as dirt, benzene, tar, naphthalene, ammonia and various form sulphur that contains in the coke oven gas after the desorption benzene, in order to satisfy coke oven gas pressure boost and carry and subsequent deep purification, reach the needs that the synthetic system of production chemicals purifies.
Optionally, as shown in fig. 2, the prewashing tower 1 includes a transmission device 101, a rotating shaft 115 and a prewashing housing 108, the transmission device 101 is connected to one end of the rotating shaft 115, the other end of the rotating shaft 115 is connected to a rotor 104, the rotor 104 is disposed at the middle lower part of the inner cavity of the prewashing housing 108, a gas outlet 107 is connected to the middle of the top of the prewashing housing 108, a liquid outlet 102 is connected to the bottom of the prewashing housing 108, a gas inlet 103 is connected to the bottom of one side of the prewashing housing 108, a liquid inlet 109 is connected to the middle upper part of the other side of the prewashing housing 108, an L-shaped liquid pipeline is connected to the liquid inlet 109, a vertical pipe of the L-shaped liquid pipeline extends to the middle of the rotor 104, a plurality of liquid nozzles 111 are mounted on the vertical pipe of the L-shaped liquid pipeline, a demister 106 is disposed at the top of the inner cavity of the prewashing housing 108, a partition plate 105 is mounted between the bottom of the demister 106 and the top of the rotor 104, a first seal 110 is disposed between the top of the rotor 104, the two sides of the middle of the bottom of the rotor 104 are sealed with the rotating shaft 115 through a second sealing gasket 112 and a third sealing gasket 113 respectively, and the interior of the rotor 104 is filled with a packing layer 114.
Optionally, as shown in fig. 3, the four-phase separator 2 includes a separation shell 218, and an inner cavity of the separation shell 218 is divided into an inlet section i, a settling separation section ii and a collection section iii from left to right; the inlet section I is provided with a gas-liquid separator 206, a baffle 207 and a calming plate 208, the feed inlet 201 is arranged outside the separation shell 218 and is connected with the top of the separation shell 218, the gas-liquid separator 206 is arranged below the feed inlet 201, the bottom end of the calming plate 208 is connected with the bottom of the separation shell 218, and the top end of the baffle 207 is connected with the top of the separation shell 218 and is positioned between the gas-liquid separator 206 and the calming plate 208; the sedimentation separation section II is provided with a coalescer 209; the collection section III is provided with a heavy phase fluid overflow weir 217, a heavy phase fluid collection groove 219, a light phase fluid collection groove 220 and an intermediate phase fluid overflow weir 216, the heavy phase fluid overflow weir 217 is arranged on one side of the coalescer 209 and is connected with the bottom of the separation shell 218, the top end of the heavy phase fluid collection groove 219 is connected with the bottom of the separation shell 218 and is positioned between the coalescer 209 and the heavy phase fluid overflow weir 217, the top and the bottom of the side wall of the heavy phase fluid collection groove 219 are respectively provided with a first liquid level meter 213, the bottom of the heavy phase fluid collection groove 219 is connected with a heavy phase fluid outlet 203, the top and the bottom of the separation shell 218 above the heavy phase fluid collection groove 219 are respectively provided with a second liquid level meter 212, the light phase fluid collection groove 220 is arranged on one side of the heavy phase fluid overflow weir 217, the front wall of the light phase fluid collection groove 220 is a light phase fluid overflow weir 214, and the height of the light phase fluid overflow weir 214 is lower than the height of the rear wall 215 of the light phase fluid collection groove 220, a third liquid level meter 210 is respectively arranged at the top and the bottom in the light phase fluid collecting tank 220, a light phase fluid outlet 204 is connected to the bottom of the light phase fluid collecting tank 220, the light phase fluid outlet 204 is positioned outside the separating shell 218, a demister 222 is arranged above the light phase fluid collecting tank 220, the gas phase outlet 202 is arranged outside the separating shell 218 and is connected with the demister 222, an intermediate phase fluid overflow weir 216 is arranged at one side of the light phase fluid collecting tank 220 and is connected with the bottom of the separating shell 218, the intermediate phase fluid overflow weir 216 and the space at the tail part of the separating shell 218 form an intermediate phase fluid collecting tank 221, a fourth liquid level meter 211 is respectively arranged at the top and the bottom at one side of the intermediate phase fluid overflow weir 216, and the intermediate phase fluid outlet 205 is connected to the bottom of the separating shell 218 at one side of the intermediate phase fluid overflow weir 216.
Wherein gas-liquid separator 206 and calming plate 208 are conventional components of inlet section i, wherein gas-liquid separator 206 has the primary function of achieving gas-liquid pre-separation, and may take a variety of forms in practical application, and functions to provide uniform initial distribution or redistribution of liquid at the top of the packing or at a certain height, to enhance the effective surface for mass and heat transfer, to improve phase-to-phase contact, and thereby to enhance the separation efficiency of the column. The main function of the static plate 208 is to slow down the two-phase fluctuation of the liquid phase region of the inlet section I, and also to have the function of liquid-liquid pre-separation, but mainly to inhibit the fluctuation to provide stable operation conditions for the sedimentation separation section II. The coalescer 209 is primarily intended to enhance the separation efficiency by promoting coalescence of the light phase (e.g., oil droplets) on the plate surface, and also has the function of suppressing fluctuation of the liquid phase region in the settling section ii.
Optionally, the length ratio of the inlet section i, the settling separation section ii and the collection section iii is 1: 3.2-4.2: 2.
optionally, the top end of the ballast plate 208 is at the same level as the second level gauge 212 at the top of the separation housing 218; the bottom end of the baffle 207 is 400 mm and 500mm higher than the top end of the sedation plate 208, and the bottom end of the baffle 207 is not less than 200mm lower than the bottom end of the gas-liquid separator 206.
Alternatively, the height of the coalescer 209 is the same as the height of the light phase fluid weir 214 (H1), the height of the heavy phase fluid weir 217 is 500mm above the bottom end of the light phase fluid collection tank 220, the height of the light phase fluid weir 214 is 1/2-3/4 of the diameter of the four phase separator, the height of the back wall 215 of the light phase fluid collection tank 220 (H2) is 200mm above the bottom end of the demister 222, and the height of the intermediate phase fluid weir 216 (H3) is 20-100mm below the height of the light phase fluid weir 214.
The three overflow weir plates of the heavy phase fluid overflow weir 217, the light phase fluid overflow weir 214 and the middle phase fluid overflow weir 216, the three heavy phase fluid collecting tanks 219, the light phase fluid collecting tank 220 and the middle phase fluid collecting tank 221 are arranged in the collecting section III, so that the length of the collecting section III of the four-phase separator 2 is larger than that of a common separator, but the liquid-liquid interface in the operation process is well controlled due to the arrangement, the stable operation of the separation process is ensured, and the influence of working condition fluctuation on the process of the sedimentation separation section II is reduced or avoided. The embodiment of the utility model provides an in the four-phase separator 2 the control at liquid-liquid interface derive from two aspects: the three overflow weir plates and the three liquid phase collecting groove structures enable a liquid-liquid interface to be simultaneously controlled by hydrostatic pressure of light phase/intermediate phase and heavy phase, so that the liquid-liquid interface is relatively stable; the light phase fluid collecting tank 220 and the intermediate phase fluid collecting tank 221 provide buffer space for fluctuation of upstream and downstream (inlet and outlet) flow in the operation process, so that influence of fluctuation of working conditions on the separation process of the settling section is reduced or avoided. By arranging the components such as the static plate 208, the coalescer 209 and the like, the liquid-liquid sedimentation separation can be realized by ensuring the lower transverse flow velocity to ensure that the liquid in the liquid phase region has enough residence time, meanwhile, the sedimentation or the buoyancy lift of the dispersed phase is facilitated, the fluctuation of the liquid phase region is also reduced, the separation time is shortened, and the size of the equipment is reduced.
The utility model discloses an all adopt four-phase separator 2 shown in FIG. 3, it includes to synthesize the influence factor that considers the pressure distribution of II terminal separation sections of actual separation operating mode subsides: the height of the light phase fluid weir 214 and the difference in height of the three weirs, the slice thickness at the weir crest and the slice flow rate at the weir crest and the flow resistance at the bottom of the light phase collection tank 220.
The pretreatment method for the deep purification of the coke oven gas of the pretreatment system for the deep purification of the coke oven gas comprises the following steps:
s1, introducing the coke oven gas after benzene elution and a gas detergent into the prewashing tower 1 through the gas phase inlet 103 and the liquid phase inlet 109 of the prewashing tower 1 respectively.
The coke oven gas after benzene elution contains impurities such as dust, benzene, tar, naphthalene, ammonia, sulfur in various forms, and the like. Wherein tar dustThe content is 5-15 mg/m3The naphthalene content is 10-200 mg/m3Ammonia content of 15-100 mg/m3The sulfur content is less than 500mg/m3。
S2, in the prewashing tower 1, the gas washing agent enters the packing layer 114 after being evenly distributed through the liquid phase nozzle 111, and under the action of the transmission device 101, the rotating shaft 115 and the rotor 104, the gas washing agent is split into liquid microelements (liquid films, liquid threads and liquid drops) and contacts with the coke oven gas after benzene elution in a countercurrent mode to remove impurities in the coke oven gas after benzene elution.
Because prewashing tower 1 is hypergravity rotary device, make the embodiment of the utility model provides an utilize hypergravity rotary technology to carry out the desorption of impurity, the cutting particle diameter of gravity rotary technology reaches 10-8m, the grain diameter of the coal gas washing agent passing through the packing layer 114 almost reaches the classification level, and the coal gas washing agent is gathered in the supergravity rotating device and then removed together with impurities. By utilizing the supergravity rotation technology, the washing effect can be enhanced, the washed particle size cutting size is reduced, and meanwhile, under the action of liquid phase spraying and supergravity, liquid drops are more uniformly distributed and have larger contact surface with impurities in the coke oven gas, so that the elution effect is improved. The supergravity rotating device has the characteristics of good particle trapping effect, small gas phase pressure drop, difficult blockage of rotating filler and the like, so that harmful substances such as dust, benzene, tar, naphthalene, ammonia and the like in the coke oven gas after benzene elution are deeply removed, the pressurization conveying and the subsequent deep purification of the coke oven gas are met, and the purification requirement of a chemical production synthesis system is met.
Practice proves that after the treatment in the mode, the dust collection efficiency reaches more than 99 percent, and particles with the particle size of more than 3 mu m can be completely removed; the removal rate of naphthalene is more than 80%; the removal rate of tar and dust is more than 60 percent, and the removal rate of organic sulfur is more than 85 percent; the removal rate of ammonia reaches more than 50 percent; the removal rate of the benzene reaches more than 50 percent.
And S3, defoaming the coke oven gas after removing the impurities by the demister 106 to obtain pretreated coke oven gas, throwing the coal gas detergent after removing the impurities to the inner wall of the prewashing shell 108, and flowing into the four-phase separator 2 through the liquid phase outlet 102.
The gas washing agent after removing impurities is rich in impurities such as tar dust, naphthalene, ammonia and the like.
S4, performing gas-liquid separation on the gas washing agent after the impurities are removed by the four-phase separator 2, pressurizing the separated intermediate phase serving as the gas washing agent by the circulating pump 3, performing heat exchange on the gas washing agent by the heat exchanger 4 to 15-20 ℃, recycling the intermediate phase serving as the gas washing agent, sending the separated light phase and heavy phase serving as products into a pipe area, and performing centralized collection and aftertreatment on the separated gas phase.
Alternatively, the operating conditions of the prewash column 1 are: the operation temperature is 15-20 ℃, the operation pressure is 3-6 kPa, and the specific surface area of the filler is 500-4000 m2/m3The filler rotating frequency is 30-60 Hz, and the gas-liquid ratio is 1000-6000.
Optionally, the porosity of the filler layer 114 is 80% to 99%; the filler of the filler layer 114 adopts large corrugated wire mesh filler and small corrugated wire mesh filler. The small corrugated filler with the length accounting for 5% -10% of the radius of the prewashing shell 108 is arranged near the rotating shaft 115, preferably 5% -8%. The average pore diameter of the large corrugated wire mesh packing is 5-10 mm, and preferably 4-8 mm; the average pore diameter of the small corrugated wire mesh packing is 1-5 mm, preferably 2-4 mm. The packing mode is beneficial to uniform atomization of liquid-phase washing liquid, the impurity trapping effect is improved, the large-ripple packing can reduce the gas-liquid phase resistance, and the anti-blocking capacity of the packing is improved.
Optionally, the gas washing agent is one or a combination of two or more of desalted water, methanol, ethanol, crude benzene, wash oil and tar.
It is to be understood that the above embodiments are merely exemplary embodiments that have been employed to illustrate the principles of the present invention, and that the present invention is not limited thereto. It will be apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit and substance of the invention, and these modifications and improvements are also considered to be within the scope of the invention.
Claims (6)
1. The pretreatment system for deep purification of coke oven gas is characterized by comprising a prewashing tower (1), a four-phase separator (2), a circulating pump (3) and a heat exchanger (4), wherein the prewashing tower (1) is a supergravity rotating device, and the four-phase separator (2) is a horizontal three-weir gas-liquid separator, wherein: a gas phase inlet (103) of the prewashing tower (1) is connected with a coke oven gas pipeline after benzene elution, a liquid phase outlet (102) of the prewashing tower (1) is connected with a feed inlet (201) of the four-phase separator (2), a middle phase fluid outlet (205) of the four-phase separator (2) is connected with a liquid inlet of the circulating pump (3), a liquid outlet of the circulating pump (3) is connected with a liquid inlet of the heat exchanger (4), and a liquid outlet of the heat exchanger (4) is connected with a liquid phase inlet (109) of the prewashing tower (1).
2. The pretreatment system for deep purification of coke oven gas according to claim 1, wherein the prewashing tower (1) comprises a transmission device (101), a rotating shaft (115) and a prewashing shell (108), the transmission device (101) is connected with one end of the rotating shaft (115), the other end of the rotating shaft (115) is connected with a rotor (104), the rotor (104) is arranged at the middle lower part of the inner cavity of the prewashing shell (108), a gas outlet (107) is connected with the middle of the top of the prewashing shell (108), a liquid outlet (102) is connected with the bottom of the prewashing shell (108), a gas phase inlet (103) is connected with the bottom of one side of the prewashing shell (108), a liquid phase inlet (109) is connected with the middle upper part of the other side of the prewashing shell (108), an L-shaped liquid pipeline is connected with the liquid inlet (109), the vertical pipe of the L-shaped liquid pipeline extends to the middle part of the rotor (104), and a plurality of liquid phase nozzles (111) are arranged on the vertical pipe of the L-shaped liquid pipeline, the top of prewashing casing (108) inner chamber is equipped with demister (106), install division board (105) between demister (106) bottom and rotor (104) top, it is sealed through first sealed pad (110) between rotor (104) top middle and division board (105), it is sealed through second sealed pad (112) and third sealed pad (113) respectively between rotor (104) bottom middle both sides and pivot (115), rotor (104) inside packing has packing layer (114).
3. The pretreatment system for deep purification of coke oven gas according to claim 1 or 2, wherein the four-phase separator (2) comprises a separation shell (218), and an inner cavity of the separation shell (218) is divided into an inlet section (I), a settling separation section (II) and a collection section (III) from left to right;
the inlet section (I) is provided with a gas-liquid separator (206), a baffle (207) and a calming plate (208), the feed inlet (201) is arranged outside the separation shell (218) and connected with the top of the separation shell (218), the gas-liquid separator (206) is arranged below the feed inlet (201), the bottom end of the calming plate (208) is connected with the bottom of the separation shell (218), and the top end of the baffle (207) is connected with the top of the separation shell (218) and is positioned between the gas-liquid separator (206) and the calming plate (208); the sedimentation separation section (II) is provided with a coalescer (209); the collecting section (III) is provided with a heavy phase fluid overflow weir (217), a heavy phase fluid collecting tank (219), a light phase fluid collecting tank (220) and a middle phase fluid overflow weir (216), the heavy phase fluid overflow weir (217) is arranged on one side of the coalescer (209) and is connected with the bottom of the separating shell (218), the top end of the heavy phase fluid collecting tank (219) is connected with the bottom of the separating shell (218) and is positioned between the coalescer (209) and the heavy phase fluid overflow weir (217), the top and the bottom of the side wall of the heavy phase fluid collecting tank (219) are respectively provided with a first liquid level meter (213), the bottom of the heavy phase fluid collecting tank (219) is connected with a heavy phase fluid outlet (203), the top and the bottom of the separating shell (218) above the heavy phase fluid collecting tank (219) are respectively provided with a second liquid level meter (212), the light phase fluid collecting tank (220) is arranged on one side of the heavy phase fluid overflow weir (217), the front wall of the light phase fluid collecting tank (220) is a light phase fluid overflow weir (214), the height of the light phase fluid overflow weir (214) is lower than that of the rear wall (215) of the light phase fluid collecting tank (220), a third liquid level meter (210) is respectively arranged at the top and the bottom in the light phase fluid collecting tank (220), the bottom of the light phase fluid collecting tank (220) is connected with a light phase fluid outlet (204), the light phase fluid outlet (204) is positioned outside the separating shell (218), a demister (222) is arranged above the light phase fluid collecting tank (220), the gas phase outlet (202) is arranged outside the separating shell (218) and is connected with the demister (222), a middle phase fluid collecting tank overflow weir (216) is arranged at one side of the light phase fluid collecting tank (220) and is connected with the bottom of the separating shell (218), the middle phase fluid overflow weir (216) and the space at the tail part of the separating shell (218) form a middle phase fluid collecting tank (221), the top and the bottom of one side of the intermediate phase fluid overflow weir (216) are respectively provided with a fourth liquid level meter (211), and the bottom of the separation shell (218) of one side of the intermediate phase fluid overflow weir (216) is connected with an intermediate phase fluid outlet (205).
4. The pretreatment system for deep purification of coke oven gas according to claim 3, wherein the length ratio of the inlet section (I), the settling separation section (II) and the collection section (III) is 1: 3.2-4.2: 2.
5. the coke oven gas deep purification pretreatment system of claim 3, wherein the top end of the ballast plate (208) is at the same level with a second liquid level meter (212) located at the top of the separation housing (218); the bottom end of the baffle (207) is 400 mm and 500mm higher than the top end of the sedation plate (208), and the bottom end of the baffle (207) is not less than 200mm lower than the bottom end of the gas-liquid separator (206).
6. The pretreatment system for deep purification of coke oven gas according to claim 3, wherein the height of the coalescer (209) is the same as the height of the light phase fluid overflow weir (214), the height of the heavy phase fluid overflow weir (217) is 500mm higher than the bottom end of the light phase fluid collection tank (220), the height of the light phase fluid overflow weir (214) is 1/2-3/4 of the diameter of the four-phase separator, the height of the rear wall (215) of the light phase fluid collection tank (220) is 200mm higher than the bottom end of the demister (222), and the height of the intermediate phase fluid overflow weir (216) is 20-100mm lower than the height of the light phase fluid overflow weir (214).
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