Tail gas adsorption and recovery device for vegetable oil leaching workshop

Abstract

The utility model discloses a tail gas adsorption and recovery device of a vegetable oil leaching workshop, and belongs to the technical field of energy-saving and consumption-reducing process systems of vegetable oil leaching workshops. According to the device, tail gas from a leaching workshop is absorbed and desorbed through equipment such as the adsorption tower and the desorption tower, so that the problems of n-hexane loss, difficulty in desorption, high steam consumption and the like during recovery are solved.

Description

Technical Field

[0001] The utility model relates to the technical field of energy-saving and consumption-reducing process systems for vegetable oil extraction workshops, and more specifically to an exhaust gas adsorption and recovery device for vegetable oil extraction workshops. Background Art

[0002] In the process of bulk oil processing, the pre-impregnation process is generally adopted, that is, after the oil is processed in the pre-treatment workshop, it is transported to the leaching workshop, and the oil in the oil is extracted by leaching. The leaching method is to apply the principle of extraction, select an organic solvent that can dissolve oil, and now mostly select n-hexane, so that it is sprayed, soaked, infiltrated, drained and other processes with the pre-treated oil, so that the oil in the oil is dissolved. A kind of oil production method. The organic solvent and the oil dissolved in it form a mixed oil. The mixed oil is evaporated and stripped by taking advantage of the different boiling points of the organic solvent and the oil, and the solvent is separated, leaving the oil to obtain crude oil. Steam containing organic solvents will be generated during the evaporation process, and the organic solvent can be recycled by condensation. To prevent the overflow of the steam, all systems such as evaporation and condensation are kept under negative pressure. However, due to the air brought in by the oil input and the air entering the system due to the poor sealing, the steam cannot be effectively condensed, so a large amount of non-condensable tail gas rich in n-hexane steam, that is, the tail gas of the leaching workshop, is generated, which needs to be further treated.

[0003] At present, in the recovery and treatment of tail gas in vegetable oil extraction workshop, the following methods are mostly used: Figure 1 The paraffin oil recovery system shown in the figure absorbs and analyzes the n-hexane in the tail gas through an absorption tower and an analysis tower to recover it. The n-hexane content in the tail gas discharged after absorption by the absorption tower will still be greater than 2000ppm, which cannot meet the emission standard of less than 60ppm, polluting the environment and causing a large amount of solvent loss. When paraffin oil is analyzed, the temperature needs to be raised to 110℃. When it is absorbed, it needs to be cooled to 30℃, which requires a large amount of steam and circulating cooling water, resulting in a large amount of energy consumption.

[0004] Chinese patent CN117815832A discloses a system for recovering medium and utilizing waste heat from tail gas in a leaching workshop, which includes an absorption tower, an analysis tower, a resin adsorption tower, a drying and cooling machine, and other equipment. The tail gas from the tail gas condenser of the leaching workshop is first absorbed by the mineral oil in the adsorption tower, and then the n-hexane is separated and recovered by the analysis tower. Among them, the tail gas after freezing and absorption in the absorption tower is sent to the resin adsorption tower for further adsorption to reduce the VOC content in the tail gas to meet the emission standards.

[0005] However, the mineral oil absorption and analysis adopted in the above technical solution to recover and discharge n-hexane is difficult to meet the requirements for low-concentration tail gas recovery in the tail gas treatment of the leaching workshop, and the analysis is difficult; it leads to large loss of n-hexane and large steam consumption in the analysis process; moreover, the resin adsorption tower is only used to treat the tail gas after absorption by the absorption tower, and the treatment capacity is low. Utility Model Content

[0006] 1. Technical problems to be solved by the utility model

[0007] In view of the problems of complicated process, large loss of n-hexane and steam consumption in the above-mentioned prior art, a tail gas adsorption recovery device for a vegetable oil leaching workshop is provided. The device absorbs and desorbs the tail gas with high n-hexane content from the leaching workshop through an adsorption tower and an adsorption resin, aiming to solve the problems of n-hexane loss, analysis difficulty and high steam consumption during recovery.

[0008] 2. Technical solution

[0009] In order to achieve the above-mentioned purpose, the technical solution provided by the utility model is:

[0010] The present application relates to a tail gas adsorption recovery device for a vegetable oil extraction workshop,

[0011] It includes tail gas cooling unit, adsorption and desorption unit, and air cooling unit;

[0012] The tail gas cooling unit and the air cooling unit are both connected to the adsorption and desorption unit;

[0013] The adsorption and desorption unit comprises an adsorption tower and a desorption tower, the adsorption tower and the desorption tower are connected in parallel, and both the adsorption tower and the desorption tower are filled with adsorption resin;

[0014] The adsorption tower comprises a bottom opening and a top opening, and the desorption tower comprises a bottom opening and a top opening;

[0015] The top opening of the adsorption tower and the top opening of the desorption tower are both connected with steam and cooling water;

[0016] The height-to-diameter ratios of the adsorption tower and the desorption tower are both 1.0 to 1.5;

[0017] The air cooling unit is connected to the top opening of the adsorption tower and the top opening of the desorption tower;

[0018] The tail gas cooling unit is connected to the top and bottom of the adsorption tower and the top and bottom of the desorption tower.

[0019] Furthermore, the number of the adsorption towers is N, and when N≥2, adjacent adsorption towers are connected in series;

[0020] The number of the desorption towers is M. When M≥2, adjacent desorption towers are connected in parallel.

[0021] Furthermore, the exhaust gas cooling unit includes an exhaust gas heat exchanger, an exhaust gas cooler, and an induced draft fan;

[0022] The exhaust gas heat exchanger comprises an air inlet 1, an air outlet 1, an air inlet 2 and an air outlet 2;

[0023] The exhaust gas cooler comprises an air inlet, an air outlet, a water inlet and a water outlet;

[0024] The air inlet 1 of the exhaust gas heat exchanger is connected to the induced draft fan, and the air outlet 1 is connected to the air inlet of the exhaust gas cooler;

[0025] The second air inlet of the tail gas heat exchanger is connected to the top of the adsorption tower and the top of the desorption tower, and the second air outlet is connected to the outside world;

[0026] The gas outlet of the tail gas cooler is connected to the bottom of the adsorption tower and the bottom of the desorption tower; the water inlet of the tail gas cooler is connected to the circulating water.

[0027] Further, the air cooling unit includes an air cooler and a conveying fan;

[0028] The air cooler comprises an air inlet, an air outlet, a water inlet and a water outlet;

[0029] The air inlet of the air cooler is connected to the conveying fan, and the air outlet is connected to the top of the adsorption tower and the top of the desorption tower respectively;

[0030] The water inlet of the air cooler is connected to the circulating water, and the water outlet is communicated with the outside.

[0031] Furthermore, the device also includes a pre-processing unit,

[0032] The pretreatment unit includes a washing tower, a water spray pump and a circulating water cooler;

[0033] The washing tower comprises an air inlet, an air outlet, a first water inlet, a second water inlet and a water outlet;

[0034] The circulating water cooler comprises a water inlet 1, a water outlet 1, a water inlet 2 and a water outlet 2;

[0035] The water inlet of the washing tower is connected to the alkaline solution, the air inlet of the washing tower is connected to the bottom of the adsorption tower and the bottom of the desorption tower respectively, and the air outlet of the washing tower is connected to the induced draft fan;

[0036] The water spray pump is connected to the water outlet of the washing tower and the water inlet of the circulating water cooler respectively;

[0037] The first water outlet of the circulating water cooler is connected to the second water inlet of the washing tower; the second water inlet of the circulating water cooler is connected to the water outlet of the tail gas cooler, and the second water outlet of the circulating water cooler is connected to the outside.

[0038] Furthermore, the pretreatment unit also includes a tail gas condenser;

[0039] The tail gas condenser comprises an air inlet, an air outlet, a water inlet, a water outlet and a liquid outlet;

[0040] The air inlet of the tail gas condenser is connected to the workshop tail gas, and the air outlet is connected to the air inlet of the washing tower;

[0041] The water inlet of the tail gas condenser is connected to cooling water, and the water outlet is connected to the outside;

[0042] The liquid outlet of the tail gas condenser is used to discharge condensed liquid.

[0043] 3. Beneficial effects

[0044] Compared with the prior art, the technical solution provided by the utility model has the following beneficial effects:

[0045] The utility model discloses an exhaust gas adsorption recovery device for a plant oil leaching workshop, in which an adsorption tower and a desorption tower are used to adsorb the exhaust gas from the leaching workshop with a high content of n-hexane. After the adsorption is completed, the n-hexane is desorbed by steam desorption. The n-hexane content in the exhaust gas after adsorption is below 60ppm, which meets the emission standard, reduces the loss of n-hexane, and reduces the use of steam. BRIEF DESCRIPTION OF THE DRAWINGS

[0046] Figure 1 A schematic diagram of the structure of a paraffin oil recovery system in the prior art;

[0047] Figure 2 This is a schematic diagram of the structure of a tail gas adsorption recovery device in a vegetable oil extraction workshop in this application.

[0048] Explanation of the symbols in the schematic diagram:

[0049] 101. cold mineral oil output pump; 102. mineral oil heat exchanger; 103. mineral oil heater; 104. analytical tower; 105. hot mineral oil output pump; 106. mineral oil cooler; 107. absorption tower; 108. tail gas condenser; 109. tail gas fan;

[0050] 01. Scrubber; 02. Induced draft fan; 03. Exhaust gas heat exchanger; 04. Exhaust gas cooler; 05. Adsorption tower; 06. Air cooler; 07. Conveying fan; 08. Water spray pump; 09 Circulating water cooler; 10. Exhaust gas condenser; 11. Desorption tower. DETAILED DESCRIPTION

[0051] In order to further understand the content of the utility model, the utility model is described in detail in conjunction with the drawings and embodiments.

[0052] The structures, proportions, sizes, etc. illustrated in the drawings of this specification are only used to match the contents disclosed in the specification for people familiar with this technology to understand and read. They are not used to limit the limiting conditions that can be implemented in this utility model, so they have no substantive technical significance. Any modification of the structure, change of the proportional relationship or adjustment of the size should still fall within the scope of the technical content disclosed in this utility model without affecting the effects and purposes that can be achieved by this utility model. Terms including ordinal numbers such as "first" and "second" can be used to explain various components or fluids, but these components and fluids are not limited by these terms. Therefore, without departing from the teachings of this disclosure, these terms are only used to distinguish the component / fluid from another component / fluid.

[0053] The utility model is further described below in conjunction with embodiments.

[0054] Example 1

[0055] Combination Figure 2 , a tail gas adsorption recovery device of a vegetable oil extraction workshop of this embodiment includes a tail gas cooling unit, an adsorption and desorption unit, and an air cooling unit;

[0056] The tail gas cooling unit and the air cooling unit are both connected to the adsorption and desorption unit; the adsorption and desorption unit comprises an adsorption tower 05 and a desorption tower 11, the adsorption tower 05 and the desorption tower 11 are connected in parallel, and the adsorption tower 05 and the desorption tower 11 are both filled with adsorption resin;

[0057] The adsorption tower 05 includes a bottom port and a top port, and the desorption tower 11 includes a bottom port and a top port; the top port of the adsorption tower 05 and the top port of the desorption tower 11 are both connected to steam and cooling water; usually, the temperature of the cooling water is 25-30°C. The height-to-diameter ratio of the adsorption tower 05 and the desorption tower 11 are both 1.0-1.5, so that the workshop exhaust gas with a higher concentration, such as the workshop exhaust gas with a normal hexane content of more than 2000ppm, can meet the emission standards after adsorption. If the height-to-diameter ratio of the adsorption tower 05 and the desorption tower 11 is too large, the pressure drop in the tower is too large, and the energy consumption of the induced draft fan 02 is high. If the height-to-diameter ratio of the adsorption tower 05 and the desorption tower 11 is too small, the floor area is large and the cross-section is too large, which can easily cause uneven distribution of the workshop exhaust gas, which is not conducive to the effective contact between the workshop exhaust gas and the adsorption resin, resulting in poor adsorption effect, and the exhaust gas cannot meet the emission standards after adsorption.

[0058] Among them, the filling rate of the adsorption resin in the adsorption tower 05 and the desorption tower 11 is 50% to 80%. The adsorption resin must meet the conditions of good selectivity, easy desorption, stable performance, non-flammability, long life, no catalytic effect, and not easy to break, such as the adsorption resin disclosed in Chinese patent CN101314124B.

[0059] As an optional embodiment, the number of adsorption towers 05 is N. When N≥2, adjacent adsorption towers 05 are connected in series. Multiple adsorption towers 05 connected in series for multiple adsorptions can effectively reduce the n-hexane content of the workshop exhaust gas. The number of desorption towers 11 is M. When M≥2, adjacent desorption towers 11 are connected in parallel, and different desorption towers 11 can be switched as needed. Specifically, the number of adsorption towers 05 and desorption towers 11 can be set according to actual conditions, and usually the number of desorption towers 11 is set to 1.

[0060] The exhaust gas cooling unit includes an exhaust gas heat exchanger 03, an exhaust gas cooler 04, and an induced draft fan 02; the exhaust gas heat exchanger 03 includes an air inlet 1, an air outlet 1, an air inlet 2, and an air outlet 2; the exhaust gas cooler 04 includes an air inlet, an air outlet, a water inlet, and a water outlet.

[0061] The air inlet 1 of the exhaust heat exchanger 03 is connected to the induced draft fan 02, and the air outlet 1 is connected to the air inlet of the exhaust cooler 04; the air inlet 2 of the exhaust heat exchanger 03 is connected to the top of the adsorption tower 05 and the top of the desorption tower 11, and the air outlet 2 is connected to the outside world;

[0062] The gas outlet of the tail gas cooler 04 is connected to the bottom of the adsorption tower 05 and the bottom of the desorption tower 11; the water inlet of the tail gas cooler 04 is connected to the circulating water. Usually, the temperature of the circulating water is 5-8°C.

[0063] The workshop exhaust gas after adsorption by the adsorption tower 05 or the desorption tower 11 meets the emission standards. The temperature of the workshop exhaust gas after adsorption is relatively low. After being connected to the exhaust gas heat exchanger 03, the washed workshop exhaust gas can be cooled for the first time, and then cooled for the second time by the exhaust gas cooler 04, realizing the recovery of cold energy and reducing the energy consumption of the exhaust gas cooler 04.

[0064] The air cooling unit includes an air cooler 06 and a conveying fan 07; the air cooler 06 includes an air inlet, an air outlet, a water inlet and a water outlet; the air inlet of the air cooler 06 is connected to the conveying fan 07, and the air outlet is respectively connected to the top of the adsorption tower 05 and the top of the desorption tower 11. The water inlet of the air cooler 06 is connected to the circulating water, and the water outlet is connected to the outside.

[0065] The conveying fan 07 conveys the cooling air to the air cooler 06, and the cooling air is cooled to about 5°C and is used to cool the adsorption resin.

[0066] The device also includes a pretreatment unit, which includes a washing tower 01, a water spray pump 08 and a circulating water cooler 09; the washing tower 01 includes an air inlet, an air outlet, a first water inlet, a second water inlet and a water outlet; the circulating water cooler 09 includes a first water inlet, a first water outlet, a second water inlet and a second water outlet.

[0067] The water inlet 1 of the washing tower 01 is connected to the alkaline solution, the air inlet of the washing tower 01 is connected to the bottom of the adsorption tower 05 and the bottom of the desorption tower 11 respectively, and the air outlet of the washing tower 01 is connected to the induced draft fan 02;

[0068] The water spray pump 08 is connected to the water outlet of the washing tower 01 and the water inlet of the circulating water cooler 09 respectively;

[0069] The first water outlet of the circulating water cooler 09 is connected to the second water inlet of the washing tower 01; the second water inlet of the circulating water cooler 09 is connected to the water outlet of the tail gas cooler 04, and the second water outlet of the circulating water cooler 09 is connected to the outside.

[0070] Alkaline solution can be added and supplemented through the water inlet 1 of the washing tower 01. The water outlet 2 of the washing tower 01 can be connected to a spray mechanism in the washing tower 01, and an alkaline solution such as sodium hydroxide solution can be sprayed through the spray mechanism. On the one hand, dust in the workshop tail gas can be washed and removed, and the influence of dust on the adsorption effect and service life of the adsorbent resin can be reduced, and the effect of deodorization can be played. On the other hand, the alkaline solution cooled by the circulating water cooler 09 can also further reduce the tail gas temperature during washing, and can also be recycled by the water spray pump 08.

[0071] Moreover, the circulating water cooler 09 can cool the circulating water after heat exchange for recycling. The water outlet 2 of the circulating water cooler 09 and the water outlet of the air cooler 06 can be connected to the outside through a pipeline, such as being recycled to the circulating water system for recycling.

[0072] The pretreatment unit further includes a tail gas condenser 10; the tail gas condenser 10 includes an air inlet, an air outlet, a water inlet, a water outlet and a liquid outlet.

[0073] The air inlet of the tail gas condenser 10 is connected to the workshop tail gas, and the air outlet is connected to the air inlet of the washing tower 01; the water inlet of the tail gas condenser 10 is connected to the cooling water, and the water outlet is connected to the outside; the liquid outlet of the tail gas condenser 10 is used to discharge the condensate.

[0074] The tail gas condenser 10 condenses the workshop tail gas to produce a part of condensate, that is, normal hexane liquid. The normal hexane liquid is discharged through the liquid outlet and recycled.

[0075] The present application also provides a process for utilizing the tail gas adsorption recovery device of the above-mentioned vegetable oil extraction workshop, comprising the following steps:

[0076] S1. Preliminary condensation and washing of tail gas: the workshop tail gas is introduced into the tail gas condenser 10, and the condensed workshop tail gas enters the washing tower 01 for washing;

[0077] S2, secondary condensation tail gas: The fan sends the washed tail gas to the tail gas heat exchanger 03 to cool it down to 15-20°C, and then passes through the tail gas cooler 04 to cool it down by 5-8°C;

[0078] S3. Adsorption of tail gas: the adsorption tower 05 and the desorption tower 11 perform tail gas adsorption and desorption regeneration.

[0079] Furthermore, step S3 is specifically as follows: the adsorption tower 05 first adsorbs the tail gas, and the desorption tower 11 does not adsorb at this time; when the adsorption tower 05 reaches the adsorption saturation state, the adsorption tower 05 stops adsorption and performs desorption regeneration, and the desorption tower 11 adsorbs the tail gas, and the adsorption saturation time of the desorption tower 11 is greater than the desorption regeneration time of the adsorption tower 05.

[0080] While the desorption tower 11 is adsorbing, the adsorption tower 05 is desorbing and regenerating. Before the desorption tower 11 reaches the adsorption saturation state, the adsorption tower 05 has completed the desorption and regeneration. When the desorption tower 11 reaches the adsorption saturation state, the desorption tower 11 stops adsorption and performs desorption and regeneration. Then the adsorption tower 05 adsorbs the tail gas. The adsorption saturation time of the adsorption tower 05 is longer than the desorption and regeneration time of the desorption tower 11, so as to facilitate re-circulation. The adsorption of the adsorption tower 05 and the desorption tower 11 can be controlled by setting a valve in the device.

[0081] Further, in step S3, the desorption regeneration includes a steam desorption step and a temperature reduction step;

[0082] The steam desorption step is to use steam purge to desorb the n-hexane adsorbed by the adsorption resin to produce a solvent-containing exhaust gas, wherein the steam temperature is 120-180° C. The solvent-containing exhaust gas is used as a steam heat source for the direct steam layer of the desorption machine connected to the adsorption tower 05 and the desorption tower 11.

[0083] The cooling step includes water cooling and air cooling to reduce the temperature of the adsorption resin to 5-10°C;

[0084] Among them, water cooling is performed first and then air cooling; water cooling is to use cooling water to cool the adsorption resin, and air cooling is to use cooling air to purge the adsorption resin.

[0085] Water cooling is performed first and then air cooling, which avoids the high energy consumption caused by using only air cooling to cool the adsorption resin and reduces costs. Moreover, when the adsorption resin is blown with cooling air after water cooling, the moisture on the adsorption resin can be taken away, which is beneficial to improving the adsorption effect of the adsorption resin when it is adsorbed again.

[0086] The process flow is as follows: the workshop tail gas with a high content of n-hexane enters the tail gas condenser 10 through the air inlet of the tail gas condenser 10 for condensation, and a small amount of n-hexane is condensed into n-hexane liquid, which can be recycled again. The condensed workshop tail gas then enters the washing tower 01 through the air inlet of the washing tower 01, and the workshop tail gas is washed to remove dust and other particulate matter.

[0087] The washed workshop exhaust gas is transported to the exhaust heat exchanger 03 through the induced draft fan 02 connected to the air inlet of the exhaust heat exchanger 03, and is cooled by heat exchange with the workshop exhaust gas adsorbed by the adsorption tower 05 or the desorption tower 11 to 15-20°C. Then, it enters the exhaust cooler 04 to cool down to 5-8°C, and then enters the adsorption tower 05 for adsorption.

[0088] When the adsorption tower 05 is adsorbing, the desorption tower 11 will not be adsorbing and will be in a standby state. As the adsorption proceeds, when the adsorption resin in the adsorption tower 05 reaches the adsorption saturation state, the adsorption tower 05 stops adsorption and starts desorption regeneration, and at this time, the desorption tower 11 starts adsorption. Before the adsorption resin in the desorption tower 11 reaches the adsorption saturation state, the adsorption resin in the adsorption tower 05 has completed desorption regeneration and is in a standby state. When the adsorption resin in the desorption tower 11 reaches the saturation state, the desorption tower 11 stops adsorption and starts desorption regeneration. At this time, the workshop exhaust gas passing through the exhaust cooler 04 enters the desorption tower 11, and does not enter the adsorption tower 05. The adsorption starts from the adsorption tower 05 in the standby state. Before the adsorption resin in the adsorption tower 05 reaches the adsorption saturation state, the adsorption resin in the desorption tower 11 has completed desorption regeneration, realizing continuous adsorption. After adsorption by the adsorption tower 05 or the desorption tower 11, the content of n-hexane in the exhaust gas discharged is reduced to below 60 ppm, meeting the emission standard, and after passing into the exhaust gas heat exchanger 03 for heat exchange, it is discharged into the atmosphere. Specifically, when the adsorption tower 05 is adsorbing, the adsorption tower is in a connected state with the exhaust gas heat exchanger 03 for heat exchange, and the desorption tower 11 is not connected with the exhaust gas heat exchanger 03; when the desorption tower 11 is adsorbing, the desorption tower 11 is in a connected state with the exhaust gas heat exchanger 03 for heat exchange, and the adsorption tower 05 is not connected with the exhaust gas heat exchanger 03.

[0089] Specifically, desorption regeneration is that steam at 120-180°C is introduced from the top of the adsorption tower 05 or the desorption tower 11, and the adsorption resin is subjected to a steam desorption step to desorb the adsorbed n-hexane, and a soluble gas is generated at the bottom of the adsorption tower 05 or the desorption tower 11, and the temperature of the soluble gas is 90-100°C. The soluble gas can be used as a heat source for the mixed desorption layer of the steam desorption machine to fully recover the steam waste heat and n-hexane. The temperature of the adsorption resin after the steam desorption step is relatively high, and it needs to be cooled to 5-10°C before it can enter the desorption state. Therefore, a cooling step is required to cool the adsorption resin. First, the adsorption resin is water-cooled with cooling water to initially cool it down. Then, the adsorption resin is cooled to about 5°C by the air cooler 06 to cool the adsorption resin, so that the adsorption resin enters the desorption state.

[0090] Water cooling is first performed and then air cooling is performed, which avoids the high energy consumption caused by using only air cooling to cool the adsorption resin and reduces costs. Moreover, after water cooling, the adsorption resin can be purged with cooling air to purge the water on the adsorption resin, so as to improve the adsorption effect of the adsorption resin when it is adsorbed again. The residual moisture in the adsorption tower 05 or the desorption tower 11 can also be purged out at the same time. If the cooling air after purging is found to meet the standards after detection, it can be directly discharged into the atmosphere through the bottom of the adsorption tower 05 or the bottom of the desorption tower 11; if it is found to be unqualified after detection, it will be transported to the washing tower 01 for re-adsorption, which further achieves standard discharge.

[0091] Based on the calculation of processing 3,000 tons of raw materials per day, the tail gas treatment capacity is 500m 3 / h, through Figure 1 The paraffin oil recovery system shown in the figure processes n-hexane emission content of 2000ppm. If it is reduced to 60ppm, about 30kg of n-hexane can be recovered every day. Moreover, the amount of steam required by the device is less than 1 ton per day, while the paraffin oil recovery system requires 4 to 5 tons of steam. Therefore, the use of this device can greatly reduce costs.

[0092] The above schematically describes the present invention and its implementation methods, which are not restrictive. The drawings show only one implementation method of the present invention, and the actual structure is not limited thereto. Therefore, if ordinary technicians in this field are inspired by it and design structural methods and embodiments similar to the technical solution without creativity without departing from the purpose of the present invention, they should all fall within the protection scope of the present invention.

Claims

1. A tail gas adsorption recovery device for a vegetable oil leaching workshop, characterized in that: It includes tail gas cooling unit, adsorption and desorption unit, and air cooling unit; The tail gas cooling unit and the air cooling unit are both connected to the adsorption and desorption unit; The adsorption and desorption unit comprises an adsorption tower (05) and a desorption tower (11), wherein the adsorption tower (05) and the desorption tower (11) are connected in parallel, and both the adsorption tower (05) and the desorption tower (11) are filled with adsorption resin; The adsorption tower (05) comprises a bottom opening and a top opening, and the desorption tower (11) comprises a bottom opening and a top opening; The top of the adsorption tower (05) and the top of the desorption tower (11) are both connected to steam and cooling water; The height-to-diameter ratios of the adsorption tower (05) and the desorption tower (11) are both 1.0 to 1.5; The air cooling unit is connected to the top of the adsorption tower (05) and the top of the desorption tower (11); The tail gas cooling unit is connected to the top and bottom of the adsorption tower (05) and the top and bottom of the desorption tower (11).

2. The tail gas adsorption recovery device for the vegetable oil extraction workshop according to claim 1, characterized in that: The number of the adsorption towers (05) is N, and when N≥2, adjacent adsorption towers (05) are connected in series; The number of the desorption towers (11) is M. When M≥2, adjacent desorption towers (11) are connected in parallel.

3. The tail gas adsorption recovery device for a vegetable oil extraction workshop according to claim 1, characterized in that: The exhaust gas cooling unit comprises an exhaust gas heat exchanger (03), an exhaust gas cooler (04), and an induced draft fan (02); The exhaust gas heat exchanger (03) comprises an air inlet 1, an air outlet 1, an air inlet 2 and an air outlet 2; The exhaust gas cooler (04) comprises an air inlet, an air outlet, a water inlet and a water outlet; An air inlet 1 of the exhaust gas heat exchanger (03) is connected to the induced draft fan (02), and an air outlet 1 is connected to an air inlet of the exhaust gas cooler (04); The second air inlet of the tail gas heat exchanger (03) is connected to the top of the adsorption tower (05) and the top of the desorption tower (11), and the second air outlet is connected to the outside; The gas outlet of the tail gas cooler (04) is connected to the bottom of the adsorption tower (05) and the bottom of the desorption tower (11); the water inlet of the tail gas cooler (04) is connected to circulating water.

4. The tail gas adsorption recovery device for a vegetable oil extraction workshop according to any one of claims 1 to 3, characterized in that: The air cooling unit comprises an air cooler (06) and a conveying fan (07); The air cooler (06) comprises an air inlet, an air outlet, a water inlet and a water outlet; The air inlet of the air cooler (06) is connected to the conveying fan (07), and the air outlet is connected to the top of the adsorption tower (05) and the top of the desorption tower (11) respectively; The water inlet of the air cooler (06) is connected to the circulating water, and the water outlet is connected to the outside.

5. The tail gas adsorption recovery device for the vegetable oil extraction workshop according to claim 4, characterized in that: The device also includes a pre-processing unit, The pretreatment unit comprises a washing tower (01), a water spray pump (08) and a circulating water cooler (09); The washing tower (01) comprises an air inlet, an air outlet, a first water inlet, a second water inlet and a water outlet; The circulating water cooler (09) comprises a water inlet 1, a water outlet 1, a water inlet 2 and a water outlet 2; The water inlet of the washing tower (01) is connected to the alkaline solution, the air inlet of the washing tower (01) is respectively connected to the bottom of the adsorption tower (05) and the bottom of the desorption tower (11), and the air outlet of the washing tower (01) is connected to the induced draft fan (02); The water spray pump (08) is connected to the water outlet of the washing tower (01) and the water inlet of the circulating water cooler (09) respectively; The first water outlet of the circulating water cooler (09) is connected to the second water inlet of the washing tower (01); the second water inlet of the circulating water cooler (09) is connected to the water outlet of the tail gas cooler (04), and the second water outlet of the circulating water cooler (09) is in communication with the outside.

6. The tail gas adsorption recovery device for the vegetable oil extraction workshop according to claim 5, characterized in that: The pretreatment unit further comprises a tail gas condenser (10); The tail gas condenser (10) comprises an air inlet, an air outlet, a water inlet, a water outlet and a liquid outlet; The air inlet of the tail gas condenser (10) is connected to the workshop tail gas, and the air outlet is connected to the air inlet of the washing tower (01); The water inlet of the tail gas condenser (10) is connected to cooling water, and the water outlet is connected to the outside; The liquid outlet of the tail gas condenser (10) is used to discharge condensed liquid.

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