CN114768487B - Circulating system for solvent recovery gas-liquid separation and wastewater reuse and operation method thereof - Google Patents
Circulating system for solvent recovery gas-liquid separation and wastewater reuse and operation method thereof Download PDFInfo
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- CN114768487B CN114768487B CN202210493292.1A CN202210493292A CN114768487B CN 114768487 B CN114768487 B CN 114768487B CN 202210493292 A CN202210493292 A CN 202210493292A CN 114768487 B CN114768487 B CN 114768487B
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- 239000007788 liquid Substances 0.000 title claims abstract description 192
- 238000000926 separation method Methods 0.000 title claims abstract description 74
- 239000002904 solvent Substances 0.000 title claims abstract description 45
- 238000011084 recovery Methods 0.000 title claims abstract description 38
- 239000002351 wastewater Substances 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 129
- 239000000945 filler Substances 0.000 claims abstract description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000012856 packing Methods 0.000 claims description 50
- 239000007789 gas Substances 0.000 claims description 40
- 230000001105 regulatory effect Effects 0.000 claims description 40
- 230000009471 action Effects 0.000 claims description 25
- 239000007921 spray Substances 0.000 claims description 22
- 238000005507 spraying Methods 0.000 claims description 12
- 238000003780 insertion Methods 0.000 claims description 10
- 230000037431 insertion Effects 0.000 claims description 10
- 239000008235 industrial water Substances 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 239000004381 Choline salt Substances 0.000 claims description 6
- 238000001802 infusion Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 230000003139 buffering effect Effects 0.000 claims description 5
- 230000001276 controlling effect Effects 0.000 claims description 5
- 238000007689 inspection Methods 0.000 claims description 5
- 238000005259 measurement Methods 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000004065 wastewater treatment Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 239000013505 freshwater Substances 0.000 abstract description 4
- 239000012071 phase Substances 0.000 description 76
- 239000002912 waste gas Substances 0.000 description 20
- 239000007791 liquid phase Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 10
- 238000009826 distribution Methods 0.000 description 6
- 238000003860 storage Methods 0.000 description 5
- 238000009792 diffusion process Methods 0.000 description 4
- 238000001514 detection method Methods 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000002238 attenuated effect Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000012074 organic phase Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012454 non-polar solvent Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000011272 standard treatment Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a circulating system for solvent recovery gas-liquid separation and wastewater reuse, which comprises a tail gas main pipe, a primary filler absorption tower and a secondary filler absorption tower; the air outlet of the first-level filler absorption tower is connected with the air inlet of the second-level filler absorption tower; the air outlet end of the production tail gas pipe is connected with the air inlet end of the first-stage solvent recovery air-liquid separation device; the air outlet end of the first-stage solvent recovery vapor-liquid separation device is connected with the air inlet of the first-stage filler absorption tower; the air outlet of the secondary filler absorption tower is connected with the air inlet of the secondary solvent recovery gas-liquid separation device; the gas outlet of the secondary solvent recovery gas-liquid separation device is connected with a lower treatment system. The invention improves the absorption efficiency of the solvent through the physical state of the equipment parts; by adopting a countercurrent mode with gas-phase feeding, the absorption water of the last stage absorption tower is added to be fresh water, and overflows to the previous stage gradually, so that the lowest concentration of VOC of the last stage tower is ensured.
Description
Technical Field
The invention relates to the field of tail gas treatment, in particular to a circulating system for solvent recovery gas-liquid separation and wastewater reuse and an operation method thereof.
Background
At present, environmental protection waste gas treatment requirements are stricter and stricter, VOC detection, particularly on-line detection and control accuracy is higher and higher, the absorption rate of the VOC is low, the waste water amount is large, and the living space pressure of enterprises is larger and larger. The equipment of the enterprise factory is basically physically absorbed through a spray tower, in the practical operation, the emission of VOC is controllable in the beginning link, the oil phase accumulated in the absorption tower is increased in the later period, the absorption efficiency of the absorption tower is reduced, the VOC contained in tail gas is increased along with the reduction, and the emission becomes uncontrollable. The existing tail gas absorbing device cannot be trapped and separated in time due to structural reasons and process reasons. The spray pump sprays water containing a large amount of COD to the top of the tower to spray, and the VOC can migrate to the tail gas tower at the next stage, so that the waste of power energy is also caused, the difficulty of standard treatment of a tail gas system is increased, the load of wastewater treatment is increased, the waste of partial materials is also caused, and the production cost is increased; the system has poor absorption stability, large usage amount of activated carbon, frequent replacement and high treatment cost of dangerous waste.
In order to ensure the improvement of the absorption rate, the absorption efficiency is improved mainly by increasing the stage number of the absorption tower, the investment of equipment and the occupation of equipment sites are increased, and the economic cost is increased.
Disclosure of Invention
In order to solve the problems, the invention discloses a circulating system for recovering solvent, separating gas from liquid and applying waste water and an operation method thereof, and the absorption efficiency of the solvent is improved through the physical state of equipment parts; and the tail gas is efficiently absorbed.
The solvent is recovered, gas and liquid are separated, and the wastewater is applied to a circulating system, which comprises a tail gas main pipe, a primary filler absorption tower and a secondary filler absorption tower; the air outlet of the first-level filler absorption tower is connected with the air inlet of the second-level filler absorption tower; the air outlet end of the production tail gas pipe is connected with the air inlet end of the first-stage solvent recovery air-liquid separation device; the air outlet end of the first-stage solvent recovery vapor-liquid separation device is connected with the air inlet of the first-stage filler absorption tower; the air outlet of the secondary filler absorption tower is connected with the air inlet of the secondary solvent recovery gas-liquid separation device; the gas outlet of the secondary solvent recovery gas-liquid separation device is connected with a lower treatment system.
Wherein the upper overflow pipe orifice and the lower overflow pipe orifice at one side of the tower pool of the first-level packing absorption tower are respectively connected with the liquid inlet pipe of the layering tank through a third valve and a fourth valve; a primary tower water outlet and a primary tower liquid return port are respectively arranged on the other side of the primary filler absorption tower pool; the water outlet of the primary tower is connected with a first liquid spraying pump; the spray layer of the primary filler absorption tower is connected with a first spray pump through a first spray pump infusion pipe; the spray layer of the secondary filler absorption tower is connected with a second spray pump through a second spray pump infusion tube; the secondary packing absorption tower pool is respectively provided with a secondary tower upper liquid outlet pipe and a secondary tower lower liquid outlet pipe; wherein the upper liquid outlet pipe of the secondary tower is connected with the lower liquid outlet pipe of the secondary tower through an eighth valve; the lower liquid outlet pipe of the second-stage tower is connected with the liquid return port of the first-stage tower through a tenth valve and a ninth valve in sequence; a liquid inlet pipe of the secondary tower connected with the bottom of the secondary solvent recovery gas-liquid separation device is connected with a liquid return port of the secondary filler absorption tower through a twelfth valve; when the regulating valve SV1001 is in a closed state and the liquid level meter LIC1002 is lower than the lower limit liquid level, the regulating valve SV1002 is opened and is connected with a liquid inlet pipe of the secondary tower through a fourteenth valve and a thirteenth valve in sequence to enable industrial water to enter the secondary packed tower.
The invention is further improved in that: wherein the liquid inlet pipe of the layering tank is communicated with the insertion pipe in the automatic layering tank; the oil outlet of the automatic layering tank is connected with the first oil phase collecting tank through a second valve; the air outlet of the automatic layering tank is connected with the air inlet of the automatic layering tank; the bottom of the automatic layering tank is connected with a layering tank liquid outlet pipe; the liquid outlet pipe of the layered tank is connected with an inverted U-shaped liquid level control pipe; wherein the height of the inverted U-shaped liquid level control pipe is 2/3 of the elevation of the automatic layering tank; wherein, the opening at the top of the inverted U-shaped liquid level control pipe is connected with the gas phase space of the automatic layering tank and the first-level packing absorption tower for gas phase balance; the liquid outlet pipe of the layered tank is connected with the liquid inlet insertion pipe of the automatic liquid separating tank through a sixth valve and a seventh valve.
The invention is further improved in that: the structure of the first-level packing absorption tower is consistent with that of the second-level packing absorption tower, wherein separation devices are arranged in tower pools of the first-level packing absorption tower and the second-level packing absorption tower, and each separation device comprises a collection bin and a separation channel; wherein a buffer steady flow disc and a plurality of special-shaped hanging strips are arranged in the collection bin; the buffer steady flow disc is provided with a plurality of liquid passing holes; wherein each special-shaped hanging strip is fixed at the bottom of the buffering steady flow disc through a hanging strip clamping piece; wherein rectangular notches are uniformly distributed at the bottom of the separation channel.
The invention is further improved in that: baffles are arranged in the first-level packing absorption tower and the second-level packing absorption tower; wherein the bottom of the baffle plate is provided with a circulation gap.
The mixed liquid after the absorption of the transmission tail gas of the packing layer of the absorption tower falls into the separating device in a free falling manner, a steady flow disc in a collecting bin gathers, and the kinetic energy generated by the free falling is attenuated under the action of the liquid layer of the steady flow disc with the thickness of about 10mm, so that the flow of the liquid is changed Cheng Wenliu from turbulent flow, the volatilization of part of the absorbed organic phase into a gas phase space is prevented, and the absorption liquid in a turbulent flow state passes through along the holes of the steady flow disc and under the action of molecular surface tension; the special-shaped hanging strips fall into a tower pool, the surfaces of the special-shaped clamping strips are horizontal stripes which are high in smoothness and have the defects of roughness and parallelism with a horizontal plane, in the falling process, under the action of the dense special-shaped strips, the absorption liquid flow speed is slowed down, the oil phase and the special-shaped strips are separated from each other like a tube bundle under the action of molecular surface tension, the oil phase and the water phase are gradually layered under the action of gravity, after reaching a separation channel, the flow speed is reduced to the minimum, the separated oil phase and the water phase form obvious layering, after passing through a rectangular notch of the separation channel, the oil phase and the water phase form a two-phase liquid layer with distinct size, and the two-phase liquid layer enters an overflow port and a liquid inlet of a spray pump.
The invention is further improved in that: under the action of a liquid level gauge LIC1004 and a regulating valve SV1004, the automatic liquid separating tank overflows and discharges the high-concentration oil phase into a second oil phase collecting tank, and layered organic wastewater flows into a liquid separating pump through a pipeline at the bottom; the outlet of the liquid dividing pump is divided into 3 branches, and the 1 st branch enters the automatic layering tank and is used when the parking is controlled by a hand valve; 2 nd path, through COD check instrument COD1001 measurement and control data, when COD is higher than the set value, regulating valve SV1001 is closed, regulating valve SV1003 is opened, enter the wastewater treatment system; the 3 rd branch is used for measuring and controlling data through a COD (chemical oxygen demand) inspection instrument COD1001, when the COD is lower than a set value, a regulating valve SV1003 is closed, the regulating valve SV1001 is opened, and the data enter a liquid inlet pipe of the secondary packing absorption tower through a rotameter LIC1003
The invention is further improved in that: the liquid outlet of the first-stage solvent recovery gas-liquid separation device is connected with a first oil phase collecting tank through a first valve.
The invention is further improved in that: the method comprises a gas phase process flow A and a liquid phase process flow B;
a gas phase process flow comprises the following steps:
a1, enabling tail gas from workshop production to enter a first solvent recovery gas-liquid separation device, enabling the organic matters to be subjected to primary recovery treatment by the production waste gas, enabling a trapped liquid phase to enter a first oil phase collecting tank under the action of the first solvent recovery gas-liquid separation device, and enabling a gas phase to enter a first-stage filler absorption tower;
a2: through the packing layer in the tower of the first-stage packing absorption tower, exchange with the circulating water driven by the first liquid spraying pump in the packing layer, organic matters in the waste gas are absorbed by the circulating water, VOC waste gas and small liquid drops in the waste gas enter the foam-catching layer at the top of the first-stage packing absorption tower of the tower through the two packing layers for gas-liquid separation, and the waste gas without liquid phase enters the second-stage packing absorption tower;
a3: the production waste gas in the second-level filler absorption tower continues to carry out the same absorption flow in the tower as the first-level filler absorption tower, and the qualified waste gas is captured and enters a second solvent recovery gas-liquid separation device;
a4, a gas-liquid separation device is recycled through a second solvent, a lower liquid phase is captured and enters a tower pool of a secondary filler absorption tower under the action of the separation device, and a gas phase enters a lower treatment system or RTO.
B, a liquid phase treatment flow; comprising the following steps:
b1, under the action of a regulating valve SV1001/1002 of an automatic control system, industrial water from an industrial water main pipe and circulating sleeve water from a liquid distribution pump enter a secondary packing absorption tower of a tower through the control flow of a rotameter LIC1004, and circulating water in the secondary packing absorption tower is subjected to mass transfer with production waste gas through two layers of packing in the tower under the action of a second liquid spraying pump, so as to trap organic matters in the production waste gas; enabling the production wastewater containing organic matters which freely falls down from the foam catching layer and the packing layer in the tower to enter a separating device of the first-stage packing absorption tower, carrying out oil phase layering at the bottom of the tower under the action of the separating device, converging the layered high-density water with water of the solvent recovery gas-liquid separating device, carrying out choked flow layering through a baffle, circulating the circulating water containing low organic matters in the tower through a second liquid injection pump, layering the organic matters of the layered oil phase again to the upper part in the tower pool, converging the layered oil phase of the separating device, and overflowing to the first-stage packing absorption tower through an overflow pipe orifice;
b2, delivering the organic matter-containing wastewater of the secondary filler absorption tower into a diffusion pipe of the primary filler absorption tower for steady flow and low flow velocity overflow diffusion pipe, carrying out physical layering, merging high-density water and high-density water layered by a separation device of the primary filler absorption tower, carrying out choked flow layering in a tower pool through a baffle, and then circulating the low-organic matter-containing circulating water in the tower through a first liquid injection pump and a filler layer and the separation device; the organic matters of the layered oil phase are layered again to the upper part in the tower pool and are converged with the oil phase layered by the separating device in the tower, and the upper overflow pipe orifice and the lower overflow pipe orifice are respectively connected with the liquid inlet pipe of the layering tank through a third valve and a fourth valve; overflowing to an automatic layering tank;
b3, the oil phase from the first-level packing absorption tower flows into an automatic layering tank through an insertion pipe, high-concentration oil phase overflows and is discharged into a first oil phase collecting tank through the height difference between an oil phase overflow port of the automatic layering tank and the top of an inverted U-shaped liquid level control pipe, and layered circulating water flows into the automatic layering tank through a pipeline at the bottom; in order to ensure high layering efficiency and self-flowing emptying of the tank, an inverted U-shaped liquid level control pipe is added at the bottom of the automatic layering tank, the height of the inverted U-shaped liquid level control pipe is 2/3 of the elevation of the automatic layering tank, and an opening at the top of the inverted U-shaped liquid level control pipe is connected with the gas phase space of the automatic layering tank and the first-level packing absorption tower for gas phase balance;
b4, the oil phase from the automatic layering tank flows into the automatic layering tank through an insertion pipe, and the automatic layering tank is under the action of a liquid level gauge LIC1004 and a regulating valve SV 1004; the automatic layering tank is provided with a high-low liquid level switch at the liquid level gauge, has high-low liquid level control, prevents the tank from being full and empty, discharges high-concentration oil phase overflow into the second oil phase collecting tank, and the layered circulating water flows into the liquid distribution pump through a pipeline at the bottom.
B5: the waste water containing organic matters from the automatic liquid separating tank passes through the liquid separating pump, and 3 branches are arranged at the outlet of the liquid separating pump, and the 1 st branch enters the automatic layering tank to be controlled by a hand valve-used when the vehicle is started and stopped; 2 nd path, through COD check instrument COD1001 measurement and control data, when COD is higher than the set value, the regulating valve SV1001 is closed, the regulating valve SV1003 is opened, enter the sewage treatment system; and the 3 rd branch is used for measuring and controlling data through a COD (chemical oxygen demand) inspection instrument COD1001, when the COD is lower than a set value, the regulating valve SV1003 is closed, the regulating valve SV1001 is opened, and the data enter the secondary packing absorption tower through the rotameter LIC 1003.
B6: industrial water from the mains is fed into the tower T1002 via the rotameter LIC1003 when the regulating valve SV1001 is closed and the level meter LIC1002 is below the lower limit level.
B7: valve control, in the equipment state of driving, manual valve operating condition: the inlet and outlet valves of the pump and the root valve of the instrument are all open; the blind plate valve is in a closed state; the bypass valve of the regulating valve group is closed, and the front valve and the rear valve are fully opened; the manual valve 1-14, the 4/5/6/10 valve is closed, the fourteenth valve 14 is regulated, and the rest is fully opened.
The beneficial effects of the invention are as follows:
the engineering installation can be carried out by adopting a traditional installation mode, and the flow stabilizer of the absorption tower of the core equipment adopts a quick-assembly design, so that the installation is convenient, the labor is saved, and the investment and the occupied area of the equipment are reduced.
The automatic control system is applied, so that the accurate detection of each index is improved, manual control is not needed, the control precision is improved, and the labor cost is reduced.
The oil phase (upper) is applied mechanically, so that the economic benefit of a factory is increased, the supply pressure of a supply chain and the storage pressure of a storage department are reduced, the storage requirement of dangerous chemicals is reduced for chemical enterprises with two points and one great point, the safety risk is reduced, and the risk is changed into controllable through technical measures.
The application of the absorption water reduces the capacity of external drainage and the use of fresh water, and reduces the sewage treatment cost.
The layering application of the oil phase (upper) reduces the actual storage amount of the fresh oil phase (upper) and reduces the storage risk; the oil phase (upper) is reused, so that the production raw material cost is reduced.
The high-efficiency absorption of tail gas provides reasonable technical support, the dielectric constant of the nonpolar solvent is very low through the polar and nonpolar characteristics of the solvent and the solute, the attractive force of electrolyte ions cannot be weakened, hydrogen bonds can not be formed with other polar molecules, and nonpolar substances are separated through a special-designed flow dividing component.
By adopting a countercurrent mode with gas-phase feeding, the absorption water of the last stage absorption tower is added to be fresh water, and overflows to the previous stage gradually, so that the lowest concentration of VOC of the last stage tower is ensured.
Drawings
FIG. 1, a system diagram of the present invention;
fig. 2, a partial enlarged view of BB in fig. 1;
FIG. 3, route distribution diagram of the automated liquid separation tank;
FIG. 4, a partial re-enlarged view of FIG. 2;
FIG. 5, a perspective view of a column sump of a secondary packed absorber column;
FIG. 6, a schematic structural view of a separation device;
FIG. 7 is a top view of a buffer flow stabilization plate.
Detailed Description
The present invention is further illustrated in the following drawings and detailed description, which are to be understood as being merely illustrative of the invention and not limiting the scope of the invention. It should be noted that the words "front", "rear", "left", "right", "upper" and "lower" used in the following description refer to directions in the drawings, and the words "inner" and "outer" refer to directions toward or away from, respectively, the geometric center of a particular component.
As shown in fig. 1 to 7, the recycling system for recycling gas-liquid separation and waste water in this embodiment includes a tail gas main pipe a, a primary filler absorption tower T1001 and a secondary filler absorption tower T1002; the air outlet of the first-level filler absorption tower T1001 is connected with the air inlet of the second-level filler absorption tower T1002; the air outlet end of the production tail gas pipe A is connected with the air inlet end of the first-stage solvent recovery air-liquid separation device E1001; the air outlet end of the primary solvent recovery vapor-liquid separation device E1001 is connected with the air inlet of the primary filler absorption tower T1001; the air outlet of the secondary filler absorption tower T1002 is connected with the air inlet of the secondary solvent recovery gas-liquid separation device E1002; the air outlet of the secondary solvent recovery gas-liquid separation device E1002 is connected with a lower-stage treatment system B.
The upper overflow pipe orifice and the lower overflow pipe orifice at one side of a tower pool of the first-level packing absorption tower T1001 are respectively connected with a liquid inlet pipe C of the layering tank through a third valve 3 and a fourth valve 4; a primary tower water outlet D and a primary tower liquid return port E are respectively arranged on the other side of the primary filler absorption tower T1001 tower pool; the primary tower water outlet D is connected with a first liquid spraying pump P1001; the spraying layer of the first-stage packing absorption tower T1001 is connected with a first spraying pump P1001 through a first spraying pump infusion pipe F; the spray layer of the secondary filler absorption tower T1002 is connected with a second spray pump P1002 through a second spray pump infusion pipe G; the secondary packing absorption tower T1002 tower pool is respectively provided with a secondary tower upper liquid outlet pipe H and a secondary tower lower liquid outlet pipe I; wherein the upper liquid outlet pipe H of the secondary tower is connected with the lower liquid outlet pipe I of the secondary tower through an eighth valve 8; the lower liquid outlet pipe I of the second-stage tower is connected with the liquid return port E of the first-stage tower through a tenth valve 10 and a ninth valve 9 in sequence; a liquid inlet pipe J of the secondary tower connected with the bottom of the secondary solvent recovery gas-liquid separation device E1002 is connected with a liquid return port of the secondary filler absorption tower T1002 through a twelfth valve 12; when the regulating valve SV1001 is in a closed state and the liquid level meter LIC1002 is lower than the lower limit liquid level, the regulating valve SV1002 is opened and is connected with the liquid inlet pipe J of the secondary tower through the rotor flowmeter IC1003, the fourteenth valve 14 and the thirteenth valve 13 in sequence, and industrial water is introduced into the secondary packed tower T1002.
The liquid outlet of the first-stage solvent recovery gas-liquid separation device E1001 is connected with a first oil phase collecting tank L through a first valve 1.
Wherein the liquid inlet pipe C of the layering tank is connected and communicated with an insertion pipe in the automatic layering tank V1001; wherein the oil outlet of the automatic layering tank V1001 is connected with the first oil phase collecting tank L through a second valve 2; an air outlet of the automatic layering tank V1001 is connected with an air inlet of the automatic layering tank V1002; the bottom of the automatic layering tank V1001 is connected with a layering tank liquid outlet pipe M; the liquid outlet pipe M of the layering tank is connected with an inverted U-shaped liquid level control pipe N; wherein the height of the inverted U-shaped liquid level control pipe is 2/3 of the elevation of the automatic layering tank V1001; wherein, the opening at the top of the inverted U-shaped liquid level control pipe N is connected with a gas phase space of the automatic layering tank V1001 and the first-level packing absorption tower T1001 for gas phase balance; the liquid outlet pipe M of the layering tank is connected with a liquid inlet insertion pipe of the automatic liquid separating tank V1002 through a sixth valve 6 and a seventh valve 7.
As shown in fig. 5-7, the structures of the primary filler absorption tower T1001 and the secondary filler absorption tower T1002 are consistent, wherein a separation device 0 is arranged in each of the tower pools of the primary filler absorption tower T1001 and the secondary filler absorption tower T1002, a separation device o is added, and the space height of the separation device from the bottom by 600mm is ensured to be full.
Wherein the separation device O comprises a collection bin O-1 and a separation channel O-2; wherein a buffer steady flow disc O-3 and a plurality of special-shaped hanging strips O-4 are arranged in the collecting bin O-1; the buffering steady flow disk O-3 is provided with a plurality of liquid passing holes; wherein each special-shaped hanging strip O-4 is fixed at the bottom of the buffering steady flow disc O-3 through a hanging strip clamping piece O-5; wherein rectangular notches O-6 are uniformly distributed at the bottom of the separation channel O-2.
A baffle P is arranged in the first-level filler absorption tower T1OO1 and the second-level filler absorption tower T1OO2; wherein the bottom of the baffle plate P is provided with a circulation gap P-1.
The mixed liquid after the absorption of the transmission tail gas of the packing layer of the absorption tower falls into the separating device in a free falling manner, a steady flow disc in a collecting bin gathers, and the kinetic energy generated by the free falling is attenuated under the action of the liquid layer of the steady flow disc with the thickness of about 10mm, so that the flow of the liquid is changed Cheng Wenliu from turbulent flow, the volatilization of part of the absorbed organic phase into a gas phase space is prevented, and the absorption liquid in a turbulent flow state passes through along the holes of the steady flow disc and under the action of molecular surface tension; the special-shaped hanging strips 0-4 fall into a tower pool, the surfaces of the special-shaped clamping strips are horizontal stripes which are high in smoothness and have concave-convex shapes and are parallel to a horizontal plane, in the falling process, under the action of the intensive special-shaped strips, the absorption liquid flow speed is slowed down, the oil phase and the special-shaped strips are separated from each other under the action of molecular surface tension like a tube bundle and gradually layered under the action of gravity, after reaching a separation channel, the flow speed is reduced to the minimum, the separated oil phase and the water phase form obvious layering, after passing through a rectangular notch of the separation channel, the oil phase and the water phase form a two-phase liquid layer with clear marks, and the two-phase liquid layer enters an overflow port and a liquid inlet of a spray pump.
Under the action of a liquid level meter LIC1OO4 and a regulating valve SV1OO4, the automatic liquid separating tank V1OO2 overflows and discharges a high-concentration oil phase into a second oil phase collecting tank Q, and layered organic wastewater flows into a liquid separating pump P1OO3 through a pipeline at the bottom; the outlet of the liquid distribution pump P1OO3 is divided into 3 branches, and the 1 st branch enters the automatic layering tank V1OO1 and is used when the vehicle is stopped under the control of a hand valve; 2 nd path, through COD checking instrument COD1OO1 measurement and control data, when COD is higher than the set value, regulating valve SV1OO1 is closed, regulating valve SV1OO3 is opened, and enters into waste water treatment system X; the 3 rd branch is used for measuring and controlling data through a COD (chemical oxygen demand) inspection instrument COD1OO1, when the COD is lower than a set value, a regulating valve SV1OO3 is closed, the regulating valve SV1OO1 is opened, and the data enter a liquid inlet pipe of a secondary packing absorption tower T1OO2 through a rotameter LIC1OO3
The operation method of the circulating system for solvent recovery gas-liquid separation and wastewater reuse comprises a gas phase process treatment flow and a liquid phase process flow;
a gas phase process flow comprises the following steps:
a1, enabling tail gas from workshop production to enter a first solvent recovery gas-liquid separation device E1OO1, enabling the organic matters to be subjected to primary recovery treatment by the waste gas, enabling the trapped liquid phase to enter a first oil phase collecting tank L under the action of the first solvent recovery gas-liquid separation device E1OO1, and enabling the gas phase to enter a first-stage filler absorption tower T1OO1;
a2: through a packing layer in a tower of the first-stage packing absorption tower T1OO1, exchanging organic matters in waste gas with circulating water driven by a first liquid spraying pump P1OO1 in the packing layer, absorbing organic matters in the waste gas by the circulating water, enabling VOC waste gas and small liquid drops in the waste gas to enter a foam-catching layer at the top of the first-stage packing absorption tower T1OO1 of the tower through two layers of packing layers for gas-liquid separation, and enabling the waste gas without liquid phase to enter a second-stage packing absorption tower T1OO2;
a3: the production waste gas in the second-level filler absorption tower T1OO2 is continuously subjected to the same absorption flow as that of the first-level filler absorption tower T1OO1 in the tower, and the qualified waste gas is captured and enters a second solvent recovery gas-liquid separation device E1OO2;
a4, a gas-liquid separation device E1OO2 is recycled through a second solvent, a lower liquid phase is captured and enters a tower pool of a secondary filler absorption tower T1OO2 under the action of a separation device O, and a gas phase enters a lower treatment system B or RTO.
B, a liquid phase treatment flow; comprising the following steps:
under the action of a regulating valve SV1OO1/1OO2 of an automatic control system, the industrial water from an industrial water main pipe K and circulating sleeve water from a liquid distribution pump P1OO3 enter a tower secondary filler absorption tower T1OO2 through a rotameter LIC1OO4 control flow, and the circulating water in the secondary filler absorption tower T1OO2 is subjected to mass transfer with production waste gas through two layers of fillers in the tower under the action of a second liquid spraying pump P1OO2 to trap organic matters in the production waste gas; the production wastewater containing organic matters, which freely falls down through a foam catching layer and a packing layer, in the tower enters a separation device O of a first-stage packing absorption tower T1OO1, oil phase layering is carried out at the bottom of the tower under the action of the separation device O, water of a layered high-density water and solvent recovery gas-liquid separation device E1OO2 is converged, choked flow layering is carried out through a baffle, circulating water containing low organic matters circulates in the tower through a second liquid spraying pump P1OO2, organic matters of layered oil phase are layered again to the upper part in a tower pool and are converged with the oil phase layered by the separation device, and overflows to the first-stage packing absorption tower T1OO1 through an overflow pipe orifice;
the wastewater containing organic matters of the second-level filler absorption tower T1OO2 is sent into a diffusion pipe of the first-level filler absorption tower T1OO1 for steady flow and low flow velocity for overflowing the diffusion pipe, physical layering is carried out, high-density water is converged with high-density water layered by a separation device of the first-level filler absorption tower T1OO1, flow blocking layering is carried out in a tower pool through a baffle plate, and then circulating water containing low organic matters is circulated in the tower through a filler layer and the separation device through a first liquid spraying pump P1OO 1; the organic matters of the layered oil phase are layered again to the upper part in the tower pool and are converged with the oil phase layered by the separating device in the tower, and the upper overflow pipe orifice and the lower overflow pipe orifice are respectively connected with a liquid inlet pipe C of the layering tank through a third valve 3 and a fourth valve 4; overflowing to an automatic layering tank V1OO1;
b3, the oil phase from the first-level filler absorption tower T1OO1 flows into an automatic layering tank V1OO1 through an insertion pipe, high-concentration oil phase overflows and is discharged into a first oil phase collecting tank L through the height difference between an oil phase overflow port of the automatic layering tank V1OO1 and the top of an inverted U-shaped liquid level control pipe N, and layered circulating water flows into the automatic layering tank V1OO2 through a pipeline at the bottom; in order to ensure high layering efficiency and tank self-flowing emptying, an inverted U-shaped liquid level control pipe N is added at the bottom of the automatic layering tank, the height of the inverted U-shaped liquid level control pipe N is 2/3 of the elevation of the automatic layering tank V1OO1, and an opening at the top of the inverted U-shaped liquid level control pipe N is connected with the gas phase space of the automatic layering tank V1OO1 and the first-level packing absorption tower T1OO1 to perform gas phase balance;
b4, the oil phase from the automatic layering tank V1OO1 flows into the automatic layering tank V1OO2 through an insertion pipe, and the automatic layering tank V1OO2 is under the action of a liquid level meter LIC1OO4 and a regulating valve SV1OO 4; the automatic layering tank V1OO2 is provided with a high-low liquid level switch at the liquid level gauge, has high-low liquid level control, prevents the tank from being full and empty, discharges high-concentration oil phase overflow into the second oil phase collecting tank Q, and the layered circulating water flows into the liquid distribution pump P1OO3 through a pipeline at the bottom.
B5: the organic matter-containing wastewater from the automatic liquid separation tank V1OO2 passes through a liquid separation pump P1OO3, 3 branches are arranged at the outlet of the liquid separation pump P1OO3, and the 1 st branch enters the automatic layered tank V1OO1 and is controlled by a hand valve to be used when the vehicle is started or stopped; 2 nd path, through COD checking instrument COD1OO1 measurement and control data, when COD is higher than the set value, regulating valve SV1OO1 is closed, regulating valve SV1OO3 is opened, and sewage treatment system is entered; and the 3 rd branch is used for measuring and controlling data through a COD (chemical oxygen demand) inspection instrument COD1OO1, when the COD is lower than a set value, the regulating valve SV1OO3 is closed, the regulating valve SV1OO1 is opened, and the data enter the secondary packing absorption tower T1OO2 through the rotameter LIC1OO 3.
B6: when the regulating valve SV1OO1 is closed and the liquid level meter LIC1OO2 is lower than the lower limit liquid level, the regulating valve SV1OO2 is opened and enters the tower T1OO2 through the rotameter LIC1OO 3.
B7: valve control, in the equipment state of driving, manual valve operating condition: the inlet and outlet valves of the pump and the root valve of the instrument are all open; the blind plate valve is in a closed state; the bypass valve of the regulating valve group is closed, and the front valve and the rear valve are fully opened; the manual valve 1-14, the valve 4/5/6/1O is closed, the valve 14 is regulated, and the rest is fully opened.
The embodiment adopts a countercurrent mode with gas-phase feeding, increases the absorption water of the last-stage absorption tower to be fresh water, gradually overflows to the former tower, ensures the lowest concentration of VOC of the last-stage tower, recycles the solvent (oil phase) again, generates economic value and realizes the aim of subsequent standard discharge, improves the efficiency of recycling the solvent, reduces the quantity of spray towers, particularly the improvement of the produced process equipment and facilities, and reduces the investment of hardware.
The technical means disclosed by the scheme of the invention is not limited to the technical means disclosed by the embodiment, and also comprises the technical scheme formed by any combination of the technical features.
Claims (3)
1. The recycling system for the solvent recovery gas-liquid separation and the wastewater reuse comprises a tail gas main pipe (A), a first-level filler absorption tower (T1001) and a second-level filler absorption tower (T1002); the air outlet of the first-level filler absorption tower (T1001) is connected with the air inlet of the second-level filler absorption tower (T1002); the air outlet end of the tail gas main pipe (A) is connected with the air inlet end of the first-stage solvent recovery air-liquid separation device (E1001); the air outlet end of the first-stage solvent recovery gas-liquid separation device (E1001) is connected with the air inlet of the first-stage filler absorption tower (T1001); the air outlet of the secondary filler absorption tower (T1002) is connected with the air inlet of the secondary solvent recovery gas-liquid separation device (E1002); the air outlet of the secondary solvent recovery gas-liquid separation device (E1002) is connected with a lower-stage treatment system (B); the method is characterized in that: wherein the upper overflow pipe orifice and the lower overflow pipe orifice on one side of a tower pool of the first-level packing absorption tower (T1001) are respectively connected with a liquid inlet pipe (C) of the layering tank through a third valve (3) and a fourth valve (4); a first-stage tower water outlet (D) and a first-stage tower liquid return port (E) are respectively arranged on the other side of the tower pool of the first-stage filler absorption tower (T1001); the first-stage tower water outlet (D) is connected with a first liquid spraying pump (P1001); the spray layer of the primary filler absorption tower (T1001) is connected with a first spray pump (P1001) through a first spray pump infusion pipe (F); the spray layer of the secondary filler absorption tower (T1002) is connected with a second spray pump (P1002) through a second spray pump infusion pipe (G); the secondary packing absorption tower (T1002) pool is respectively provided with a secondary tower upper liquid outlet pipe (H) and a secondary tower lower liquid outlet pipe (I); wherein the upper liquid outlet pipe (H) of the secondary tower is connected with the lower liquid outlet pipe (I) of the secondary tower through an eighth valve (8); wherein a lower liquid outlet pipe (I) of the second-stage tower is connected with a liquid return port (E) of the first-stage tower through a tenth valve (10) and a ninth valve (9) in sequence; a liquid inlet pipe (J) of the secondary tower connected with the bottom of the secondary solvent recovery gas-liquid separation device (E1002) is connected with a liquid return port of the secondary filler absorption tower (T1002) through a twelfth valve (12); when the regulating valve SV1001 is in a closed state and the liquid level meter LIC1002 is lower than the lower limit liquid level, the regulating valve SV1002 is opened and is connected with a liquid inlet pipe (J) of the secondary tower through a fourteenth valve (14) and a thirteenth valve (13) in sequence to enable industrial water to enter the secondary packing tower (T1002); wherein the liquid inlet pipe (C) of the layering tank is connected and communicated with an insertion pipe in the automatic layering tank (V1001); wherein the oil outlet of the automatic layering tank (V1001) is connected with the first oil phase collecting tank (L) through a second valve (2); the air outlet of the automatic layering tank (V1001) is connected with the air inlet of the automatic layering tank (V1002); the bottom of the automatic layering tank (V1001) is connected with a layering tank liquid outlet pipe (M); an inverted U-shaped liquid level control pipe (N) is connected to the liquid outlet pipe (M) of the layered tank; wherein the height of the inverted U-shaped liquid level control pipe is 2/3 of the elevation of the automatic layering tank (V1001); wherein, the opening at the top of the inverted U-shaped liquid level control pipe (N) is connected with the gas phase space of the automatic layering tank (V1001) and the first-level packing absorption tower (T1001) for gas phase balance; the liquid outlet pipe (M) of the layering tank is connected with a liquid inlet insertion pipe of the automatic liquid separating tank (V1002) through a sixth valve (6) and a seventh valve (7); the structure of the primary filler absorption tower (T1001) is consistent with that of the secondary filler absorption tower (T1002), wherein separation devices (0) are arranged in the tower pools of the primary filler absorption tower (T1001) and the secondary filler absorption tower (T1002), and each separation device (0) comprises a collection bin (0-1) and a separation channel (0-2); wherein a buffer steady flow disc (0-3) and a plurality of special-shaped hanging strips (0-4) are arranged in the collecting bin (0-1); a plurality of liquid passing holes are formed in the buffering steady flow disc (0-3); wherein each special-shaped hanging strip (0-4) is fixed at the bottom of the buffering steady flow disc (0-3) through a hanging strip clamping piece (0-5); wherein rectangular notches (0-6) are uniformly distributed at the bottom of the separation channel (0-2).
2. The recycling system for recycling gas-liquid separation and waste water according to claim 1, wherein: baffles (P) are arranged in the first-level packing absorption tower (T1001) and the second-level packing absorption tower (T1002); wherein the bottom of the baffle plate (P) is provided with a circulation gap (P-1).
3. The recycling system for recycling gas-liquid separation and waste water according to claim 1, wherein: under the action of a liquid level gauge LIC1004 and a regulating valve SV1004, the automatic liquid separating tank (V1002) overflows and discharges a high-concentration oil phase into a second oil phase collecting tank (Q), and layered organic wastewater flows into a liquid separating pump (P1003) through a pipeline at the bottom; 3 branches are arranged at the outlet of the liquid dividing pump (P1003), and the 1 st branch enters an automatic layering tank (V1001) and is used when the parking is controlled by a hand valve; 2 nd path, through COD check instrument COD1001 measurement and control data, when COD is higher than the set value, regulating valve SV1001 is closed, regulating valve SV1003 is opened, enter the waste water treatment system (X); the 3 rd branch is used for measuring and controlling data through a COD (chemical oxygen demand) inspection instrument COD1001, when the COD is lower than a set value, a regulating valve SV1003 is closed, the regulating valve SV1001 is opened, and the data enter a liquid inlet pipe of a secondary packing absorption tower (T1002) through a rotameter LIC 1003; the liquid outlet of the first-stage solvent recovery gas-liquid separation device (E1001) is connected with a first oil phase collecting tank (L) through a first valve (1).
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