CN220939130U - Concentrated spent acid joins in marriage sour device - Google Patents
Concentrated spent acid joins in marriage sour device Download PDFInfo
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- CN220939130U CN220939130U CN202322553449.8U CN202322553449U CN220939130U CN 220939130 U CN220939130 U CN 220939130U CN 202322553449 U CN202322553449 U CN 202322553449U CN 220939130 U CN220939130 U CN 220939130U
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- 239000002253 acid Substances 0.000 title claims abstract description 238
- 238000001704 evaporation Methods 0.000 claims abstract description 58
- 238000003860 storage Methods 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000007789 sealing Methods 0.000 claims abstract description 13
- 238000000889 atomisation Methods 0.000 claims abstract description 11
- 230000007246 mechanism Effects 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims abstract description 7
- 230000008020 evaporation Effects 0.000 claims description 52
- 230000000694 effects Effects 0.000 claims description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000009826 distribution Methods 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 229910002804 graphite Inorganic materials 0.000 claims description 5
- 239000010439 graphite Substances 0.000 claims description 5
- 239000002002 slurry Substances 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000002699 waste material Substances 0.000 abstract description 34
- 238000002360 preparation method Methods 0.000 abstract description 27
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000011085 pressure filtration Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 18
- 230000008569 process Effects 0.000 description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 9
- 238000003825 pressing Methods 0.000 description 7
- 230000009467 reduction Effects 0.000 description 6
- 239000012530 fluid Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000005304 joining Methods 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 230000005856 abnormality Effects 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- -1 ferrous monohydrate Chemical class 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a concentrated waste acid preparing device, and belongs to the technical field of waste acid recycling. The utility model solves the problems of higher temperature of waste acid after double-effect concentration and 98% acid waste caused by filtering after acid preparation in the prior art, and comprises a concentrating device, wherein the concentrating device comprises a double-effect concentrating device, the double-effect concentrating device comprises a first-effect evaporating loop, a second-effect evaporating loop and an atomization condenser, the discharge end of the second-effect evaporating loop is connected with a third-effect evaporating loop, the third-effect evaporating loop is connected with the atomization condenser, the discharge end of the third-effect evaporating loop is connected with a concentrated acid liquid sealing groove, the concentrated acid liquid sealing groove is connected with a concentrated acid storage tank, the discharge end of the concentrated acid storage tank is connected with a filtering device, and the filtering device is connected with an acid preparation mechanism. The utility model adds a three-effect step, and the temperature of the two-effect acid can be reduced by concentrating the two-effect acid again, so that the production of the subsequent acid preparation working section is facilitated, the acid preparation is carried out after the acid is concentrated and is subjected to pressure filtration, the acid preparation temperature is reduced, and the waste of 98% of acid is reduced.
Description
Technical Field
The utility model belongs to the technical field of waste acid recycling, and particularly relates to a concentrated waste acid preparing device.
Background
The waste acid treatment modes mainly comprise two modes: firstly, partial concentrated pre-acid is used for replacing 98% acid in acidolysis leaching, so that the acid consumption of acidolysis is saved by 98%; secondly, the mixed solution is prepared into 55% acid with 98% acid, 1/3 of the mixed solution is used for acidolysis and premixing, and 2/3 of the mixed solution is processed by the phosphating industry. We used all spent acid minus acidolysis leaching to formulate 55% acid with 98% acid. The waste acid is subjected to heat exchange through the waste heat of the calcination tail gas to improve the concentration of the waste acid, the yield of the calcination tail gas is limited, the waste acid cannot be fully concentrated, the acid concentration is lower by about 24.5%, 98% of acid consumption is higher, the proportion of the waste acid in 55% of acid is small, the waste acid cannot be fully recycled, and part of the waste acid still needs to be sent to a sewage station for neutralization, so that a double-effect concentration device is adopted to further concentrate the waste acid, the acid unit consumption of 98% of acid prepared by acid after concentration is also reduced, the proportion of the waste acid in 55% of acid is increased, the utilization rate of the waste acid is increased, and the cost is reduced.
However, the waste acid after double-effect concentration has higher temperature, and as the concentration of the waste acid is increased, the solubility of impurities represented by iron is reduced, and the impurities are separated out in a solid state, wherein the main component is ferrous monohydrate (accounting for about 62 percent of the total solid content), which is called ferrous flavum. The solid content of the concentrated acid is up to about 27%, if the concentrated acid is directly used for preparing 55% acid with 98% acid and then filtering is carried out, the free acid taken away in Huang Yatie accounts for 11.67% of the total amount of Huang Yatie, and the part of free acid contains a certain amount of 98% acid besides waste acid, so that the 98% acid consumption is wasted.
Disclosure of utility model
Aiming at the problems of 98% acid waste caused by high temperature of waste acid after double-effect concentration and Huang Yatie filtering and removing after acid preparation in the prior art, the utility model provides a concentrated waste acid preparation device.
The technical scheme adopted by the utility model is as follows:
The utility model provides a concentrated spent acid joins in marriage sour device, includes enrichment facility, enrichment facility includes double-effect enrichment facility, double-effect enrichment facility includes one effect evaporation circuit, two effect evaporation circuit and atomizing condenser, the discharge end of two effect evaporation circuit is connected with three effect evaporation circuit, three effect evaporation circuit is connected with atomizing condenser, the discharge end of three effect evaporation circuit is connected with concentrated acidizing fluid seal groove, concentrated acidizing fluid seal groove is connected with concentrated acid storage tank, the discharge end of concentrated acid storage tank is connected with filter equipment, filter equipment's discharge end is connected with the feed end of joining in marriage sour mechanism.
After the technical scheme is adopted, the concentrated acid is filtered and then is subjected to acid preparation, the temperature of the filtered concentrated acid is low, the acid preparation temperature is reduced, the curing period is greatly reduced, 4 hours can be saved by one batch, the capacity of a curing tank is increased, meanwhile, the power consumption is also saved, the concentrated acid is subjected to independent pressure filtration, all free acid in Huang Yatie is waste acid, and the waste of 98% acid is reduced. The method is added with a three-effect step, and the three-effect step has the main effects of concentrating the two-effect acid again to improve the acid concentration, and can greatly reduce the temperature of the two-effect acid, thereby being convenient for the production of the subsequent acid preparation working section. After the acid concentration is increased by three-effect, 98% of high-concentration acid is added less in the subsequent acid preparation working section when the acid concentration is increased, so that the cost is reduced; meanwhile, the acid concentration is further increased and then mixed with 98 percent of acid, so that the heat release is less, and the corrosion to acid preparing equipment is reduced; the acid temperature of the concentrated acid is reduced through the three-effect step, the corrosion and high-temperature deformation of the filter cloth of the preparation tank and the filter press are reduced during acid preparation, and the problem of the reduction of the service life of the filter press caused by the higher acid temperature after the pressure filtration step is carried out before and after the acid preparation is avoided.
Preferably, a heat exchanger is arranged between the concentrated acid sealing tank and the concentrated acid storage tank, the feeding end of the heat exchanger is connected with the concentrated acid sealing tank, and the discharging end of the heat exchanger is connected with the concentrated acid storage tank.
After adopting this technical scheme, cooling down again through the heat exchanger to the acid after the concentration, the acid temperature greatly reduced after the preliminary cooling down through the concentrated step of triple effect this moment, consequently the energy consumption of heat exchanger also correspondingly reduces.
Preferably, the heat exchanger is a graphite heat exchanger.
Preferably, the filter device is a filter press.
Preferably, the double-effect concentration device comprises an original acid storage tank, a preheater A, a first-effect evaporation loop, an interstage serial pump, a preheater B and a second-effect evaporation loop which are sequentially connected, wherein the first-effect evaporation loop is connected with an atomization condenser, the atomization condenser is connected with a water cooling tower, the first-effect evaporation loop is also connected with a condensation water tank, and the second-effect evaporation loop is connected with the atomization condenser and the condensation water tank.
Preferably, the two-effect evaporation loop is connected with a raw steam supply pipeline, and a steam outlet of the two-effect evaporation loop is connected with the one-effect evaporation loop through a pipeline.
Preferably, the acid preparing mechanism comprises an acid preparing tank, the feeding end of the acid preparing tank is connected with the discharging end of the filter press, the feeding end of the acid preparing tank is also connected with a 98% acid liquid supply pipeline, and the discharging end of the acid preparing tank is connected with a 55% acid slurry collecting tank.
In summary, due to the adoption of the technical scheme, the beneficial effects of the utility model are as follows:
1. Acid is prepared after acid filter pressing after concentration, the acid temperature after concentration is low after filter pressing, the acid preparation temperature is reduced, the curing period is greatly reduced, the energy of a curing tank is increased by about 4 hours, the power consumption is also saved, the acid is independently filter pressed after concentration, all free acid in Huang Yatie is waste acid, and the waste of 98% acid is reduced.
2. The method has the advantages that the method is additionally provided with the three-effect step, the three-effect step has the main effects of concentrating the two-effect acid again to improve the acid concentration, greatly reducing the temperature of the two-effect acid, facilitating the production of the subsequent acid preparation working section, reducing the acid temperature of the concentrated acid through the three-effect step, reducing the corrosion and high-temperature deformation of the filter cloth of the preparation tank and the filter press during acid preparation, and avoiding the problem of reduced service life of the filter press caused by higher acid temperature after the concentration after the filter pressing step is put before and after acid preparation.
Drawings
The utility model will now be described by way of example and with reference to the accompanying drawings in which:
FIG. 1 is a schematic diagram of the connection structure of the concentrating device according to the present utility model;
FIG. 2 is a schematic diagram of the connection structure of the acid mechanism in the present utility model.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present application more apparent, the technical solutions of the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present application, and it is apparent that the described embodiments are only some embodiments of the present application, not all embodiments. The components of the embodiments of the present application generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the application, as presented in the figures, is not intended to limit the scope of the application, as claimed, but is merely representative of selected embodiments of the application. All other embodiments, which can be made by a person skilled in the art without making any inventive effort, are intended to be within the scope of the present application.
In describing embodiments of the present utility model, it should be noted that the terms "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. refer to an azimuth or a positional relationship based on that shown in the drawings, or that the inventive product is conventionally put in place when used, merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the apparatus or elements referred to must have a specific azimuth, be configured and operated in a specific azimuth, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," "third," and the like are used merely to distinguish between descriptions and should not be construed as indicating or implying relative importance.
The present utility model is described in detail below with reference to fig. 1-2.
The utility model provides a concentrated spent acid joins in marriage sour device, includes enrichment facility, enrichment facility includes double-effect enrichment facility, double-effect enrichment facility includes one effect evaporation circuit, two effect evaporation circuit and atomizing condenser, the discharge end of two effect evaporation circuit is connected with three effect evaporation circuit, three effect evaporation circuit is connected with atomizing condenser, the discharge end of three effect evaporation circuit is connected with concentrated acidizing fluid seal groove, concentrated acidizing fluid seal groove is connected with concentrated acid storage tank, the discharge end of concentrated acid storage tank is connected with filter equipment, filter equipment's discharge end is connected with the feed end of joining in marriage sour mechanism.
In this embodiment, be provided with the heat exchanger between concentrated acid sealing tank and the concentrated acid storage tank, the feed end and the concentrated acid sealing tank of heat exchanger are connected, the discharge end and the concentrated acid storage tank of heat exchanger are connected.
In this embodiment, the heat exchanger is a graphite heat exchanger.
In this embodiment, the filtering device is a filter press.
In this embodiment, the double-effect concentration device includes the primitive acid storage tank, the pre-heater A, first effect evaporation circuit, interstage tandem pump, pre-heater B and the second effect evaporation circuit that connect gradually, first effect evaporation circuit is connected with the atomizing condenser, the atomizing condenser is connected with the cooling tower, first effect evaporation circuit still is connected with the condensate tank, second effect evaporation circuit is connected with atomizing condenser and condensate tank.
In this embodiment, the two-effect evaporation loop is connected with a raw steam supply pipeline, and a steam outlet of the two-effect evaporation loop is connected with the one-effect evaporation loop through a pipeline.
In this embodiment, the acid preparing mechanism comprises an acid preparing tank, the feeding end of the acid preparing tank is connected with the discharging end of the filter press, the feeding end of the acid preparing tank is also connected with a 98% acid liquid supply pipeline, and the discharging end of the acid preparing tank is connected with a 55% acid slurry collecting tank.
Referring to fig. 1-2, the specific method of use of the present utility model is as follows:
The dilute waste acid in the water washing process enters an original acid storage tank, is pumped to a preheater A by the original acid, and enters a one-effect evaporation loop after being preheated by the condensed water of an evaporator. The acid liquor is subjected to indirect heat exchange in a heater of a first-effect evaporation loop by subacidity secondary steam generated by second-effect evaporation, and enters a first-effect evaporator for dehydration. Then pumping the acid liquor into a preheater B by an interstage series pump, exchanging heat with the condensed water of the evaporator, entering a double-effect evaporation loop, indirectly heating and heating the acid liquor in a heater of the double-effect circulation loop by outer tube raw steam passing through a temperature and pressure reducer, and entering the double-effect evaporator for dehydration; the second-effect concentrated acid overflows into a three-effect evaporation loop, flows automatically into a transfer liquid sealing tank after adiabatic flash evaporation dehydration and cooling, and materials in the liquid sealing tank are pumped into a graphite heat exchanger for cooling and heat exchange and then enter a concentrated acid storage tank, and finally are conveyed to a filter press for filter pressing through a transfer pump and then are sent to an acid distribution station.
The specific operation steps are as follows: 1 preparation of dilute waste acid:
1.1 after closing the original acid storage tank outlet valve and the bottom drain valve, opening the original acid storage tank acid inlet pipeline valve.
1.2, Notifying titanium recovery post personnel to send acid to a waste acid concentration post.
1.3, After receiving the notification of stopping acid delivery, notifying titanium recovery post personnel to close a pump outlet valve, stopping the pump, closing a pump inlet valve, and finally closing an acid inlet pipeline valve of an original acid storage tank.
2 Steam temperature and pressure reducing system start-up
2.1 Opening inlet and outlet valves of the steam sub-cylinder, closing a steam emptying valve of the evaporator, opening a main steam pipe of the waste acid concentration system and drain valves of the sub-cylinder, and draining condensed water in a steam pipeline and the steam sub-cylinder.
2.2 Closing a manual valve for reducing temperature and pressure water, after draining condensed water, setting the steam pressure of the temperature and pressure reducer according to the process requirement on a DCS temperature and pressure reducing picture, setting the pressure as cascade, and setting the temperature as automatic.
2.3, Slowly opening a manual valve on a main steam pipe of the waste acid supply concentration system, preheating a pipeline, and gradually opening the manual valve after the pipeline temperature rises and the pipeline has no water hammer phenomenon; in the steam opening process, the steam electric valve is automatically opened and the steam pressure is regulated within a set range.
2.4 Starting the temperature-reducing water pressurizing pump, and opening the manual valve after the water pressurizing valve is opened after the pump runs normally.
2.5 On the temperature control of the DCS temperature and pressure reduction picture, the temperature set value is gradually adjusted, the stable operation of the temperature reduction electric valve is ensured, and the large temperature fluctuation of the steam pipeline is prevented. The temperature after temperature and pressure reduction is controlled by adjusting the opening of the temperature reduction water valve to meet the process requirements.
2.6, Opening the steam electric valve of the two-effect evaporation system to 30%, detecting whether the concentration of the concentrated acid reaches the process requirement after the operation is carried out for a period of time, and adjusting the opening of the steam electric valve according to the concentration.
3 Start-up of waste acid concentration system
3.1, After the first-effect bottom communicating valve to the second-effect bottom communicating valve is opened, an outlet valve of an original acid storage tank is opened, a concentrated pre-acid feeding pump is started to add dilute sulfuric acid to the system, an overflow pipe of the three-effect evaporator overflows to about 1.5m above an acid inlet of a concentrated acid liquid sealing tank, and a feeding pump is stopped. And closing the first and second effect bottom communicating valves.
And 3.2, respectively starting two forced circulation pumps according to the specification, wherein the raw material acid liquor is forced to circulate and exchange heat in each loop. And then the atomization condenser is started according to the specifications (the upper and lower water pumps of the acid circulating water and the fan of the cooling tower are started, the opening of the outlet valve of the upper water pump is adjusted, and the water inlet pressure of the spray atomization condenser meets the process requirements), so that the negative pressure of the first effect and the second effect meets the process requirements. (by controlling the opening of the valve that connects the vapor phase to the negative pressure pipe in the outlet line of the one-effect heater condenser.)
3.3, Opening a steam inlet control valve of the two-effect heater, adjusting the opening to 30%, exhausting steam by an exhaust valve of the two-effect heater for 2min, and closing. The acid liquor of the two-effect circulation loop is heated, and the steam inlet quantity is regulated so that the heating speed of the two-effect heater is strictly controlled within the process requirement range.
3.4 When the two-effect circulation loop starts to evaporate, the inlet steam temperature of the one-effect heater starts to rise, the liquid level of the two-effect evaporator starts to drop, and the two-effect circulation loop is indicated to enter an evaporation running state. The produced secondary slightly acidic steam starts to supply steam to the primary heater for heat exchange and heats the acid liquor of the primary circulation loop. The steam inlet quantity of the two-effect heater and the feeding quantity of the system are controlled, so that the heating speed of the one-effect heater is strictly controlled within the process requirement range.
3.5 The first effect level is controlled by the raw acid feed pump and the first effect evaporator level gauge, and the second effect level is controlled by the interstage series pump and the second effect evaporator level gauge.
And 3.6, after the second effect enters normal evaporation, starting an original acid feed pump and a first-effect and second-effect interstage serial pump in time to slowly convey dilute sulfuric acid to the system according to the condition of liquid level reduction in the evaporator, and keeping the first-effect evaporator and the second-effect evaporator at normal liquid levels. When the second-effect concentration reaches the process requirement, the flow of the feeding pump is gradually increased to the range of the feeding flow for normal production.
And 3.7, after the device enters a normal operation state, the condensate tank and the interstage preheater on the flow line are automatically put into operation along with the normal operation of each evaporation loop. The water outlet control valve of the inter-stage preheater is closely watched to stably control the liquid level of the condensed water collecting tank within the range of process requirements. If the repair is not possible, the manual control is changed into the automatic control after the repair is performed, and the electric instrument worker is informed of checking the repair immediately.
And 3.8, closely paying attention to the temperature, pressure and liquid level change of the gas phase and the liquid phase of the evaporator in the operation process. And measures are taken in time to adjust operation process parameters, so that the safe and economic operation of the device is ensured.
And 3.9, when the concentration of the sulfuric acid in the liquid seal tank meets the process requirement, starting a conveying pump to convey the concentrated sulfuric acid into a concentrated acid graphite heat exchanger, and enabling the cooled finished acid to enter a concentrated acid storage tank.
And 3.10, filling in a post original record table, and correcting at any time according to the change of the operating parameters of the instrument, so that the system is in a normal state, and the concentrated acid finished product is ensured to continuously overflow into the liquid seal groove. Meanwhile, the system is checked on site at intervals of two hours (according to the execution of a tour inspection table), and measures are taken in time when abnormality is found, so that the system is ensured to run normally.
3.11 Connecting an acid distribution station, opening an outlet valve of a concentrated acid storage tank after confirming that the concentrated acid can be conveyed, opening an inlet valve of a concentrated acid pump, starting the concentrated acid pump, opening an outlet valve of the pump, and conveying acid to the acid distribution station; and after receiving the notification of stopping acid delivery, closing the valve of the pump outlet, stopping the pump, and closing the valve of the pump inlet.
And 3.12, filling in the working conditions of the production, equipment and instruments in the shift, such as the record of the actual shift, and improving the civilization and sanitation of the post.
3.13 When the pump outlet pressure of the forced circulation pump of the system is more than 0.28Mpa or the running current is more than 150A, the system is cleaned by stopping the system and inorganic salt is deposited and the equipment is checked and overhauled.
4, Acid preparation after concentrated acid filter pressing:
4.1, opening a circulating cooling water inlet and outlet valve of the concentrated acid transfer tank, opening an acid inlet manual valve, closing a bottom outlet valve, connecting a waste acid concentration station to feed acid to the transfer tank, and starting stirring after the liquid level reaches a stirring lower blade.
4.2 The liquid level of the concentrated acid transfer tank is not more than 4.5m, and the concentrated acid transfer tank can be filter-pressed after the liquid level exceeds 2.0 m.
And opening a manual valve and an electric valve at the root of the concentrated acid transfer tank, opening an outlet valve of a feed pump by 30%, opening a concentrated acid feed pneumatic valve of a filter press, closing a 55% acid feed pneumatic valve, opening a concentrated acid discharge pneumatic valve of the filter press, closing a 55% acid discharge pneumatic valve, and closing a manual valve and an electric valve at the root of the concentrated acid distribution tank. Starting the feeding pump to start feeding, and gradually opening the manual valve of the pump outlet to full open after starting the pump.
4.3, After the filter-pressing concentrated acid filtrate enters the acid preparation tank, opening a valve of a circulating cooling water inlet and outlet of the acid preparation tank, starting stirring after the liquid level submerges a stirring blade, stopping filter-pressing after the liquid level reaches 3.0-3.2 m, adding 98% of acid with the required amount of the process into the acid preparation tank, and controlling the final acid concentration to be 53.0% -56.0%.
4.4, When the acid temperature of the acid preparation tank is reduced to the range of the technological requirement, opening a root valve of the acid preparation tank, placing the slurry into a 55% acid slurry collecting tank, and closing the root valve after the acid in the acid preparation tank is completely discharged.
5, Connecting the post of the sulfuric acid large warehouse, preparing to receive 55% acid, opening the bottom outlet valve of the 55% acid transfer tank after the acid inlet valve of the 55% acid large warehouse is opened, opening the inlet valve of the 55% acid pump, starting the pump, slowly opening the outlet valve of the pump, delivering 55% acid to the 55% acid large warehouse, closing the outlet valve of the 55% acid pump after delivering materials, and stopping the pump; and opening the outlet valve of the pump, closing the inlet valve and the outlet valve of the pump after the acid in the pipeline is refluxed, and closing the outlet valve of the 55% acid transfer tank.
3.2.6 Bringing the sewage in the acidic wastewater collection tank to a sewage treatment station at irregular intervals.
The above examples merely illustrate specific embodiments of the application, which are described in more detail and are not to be construed as limiting the scope of the application. It should be noted that it is possible for a person skilled in the art to make several variants and modifications without departing from the technical idea of the application, which fall within the scope of protection of the application.
Claims (7)
1. The utility model provides a concentrated spent acid joins in marriage sour device, includes enrichment facility, enrichment facility includes double-effect enrichment facility, double-effect enrichment facility includes one effect evaporation circuit, two effect evaporation circuit and atomizing condenser, its characterized in that: the discharge end of the second-effect evaporation loop is connected with a third-effect evaporation loop, the third-effect evaporation loop is connected with an atomization condenser, the discharge end of the third-effect evaporation loop is connected with a concentrated acid sealing tank, the concentrated acid sealing tank is connected with a concentrated acid storage tank, the discharge end of the concentrated acid storage tank is connected with a filter device, and the discharge end of the filter device is connected with the feed end of the acid distribution mechanism.
2. The concentrated spent acid distribution device according to claim 1, wherein: a heat exchanger is arranged between the concentrated acid sealing tank and the concentrated acid storage tank, the feeding end of the heat exchanger is connected with the concentrated acid sealing tank, and the discharging end of the heat exchanger is connected with the concentrated acid storage tank.
3. The concentrated spent acid distribution device according to claim 2, characterized in that: the heat exchanger is a graphite heat exchanger.
4. A concentrated spent acid distribution device according to any one of claims 1-3, characterized in that: the filtering device is a filter press.
5. A concentrated spent acid distribution device according to any one of claims 1-3, characterized in that: the double-effect concentration device comprises an original acid storage tank, a preheater A, a first-effect evaporation loop, an interstage serial pump, a preheater B and a second-effect evaporation loop which are sequentially connected, wherein the first-effect evaporation loop is connected with an atomization condenser, the atomization condenser is connected with a water cooling tower, the first-effect evaporation loop is also connected with a condensation water tank, and the second-effect evaporation loop is connected with the atomization condenser and the condensation water tank.
6. The concentrated spent acid distribution device according to claim 5, wherein: the two-effect evaporation loop is connected with a raw steam supply pipeline, and a steam outlet of the two-effect evaporation loop is connected with the one-effect evaporation loop through a pipeline.
7. A concentrated spent acid distribution device according to any one of claims 1-3, characterized in that: the acid preparing mechanism comprises an acid preparing tank, the feeding end of the acid preparing tank is connected with the discharging end of the filter press, the feeding end of the acid preparing tank is also connected with a 98% acid liquid supply pipeline, and the discharging end of the acid preparing tank is connected with a 55% acid slurry collecting tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322553449.8U CN220939130U (en) | 2023-09-20 | 2023-09-20 | Concentrated spent acid joins in marriage sour device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322553449.8U CN220939130U (en) | 2023-09-20 | 2023-09-20 | Concentrated spent acid joins in marriage sour device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220939130U true CN220939130U (en) | 2024-05-14 |
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ID=91004952
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322553449.8U Active CN220939130U (en) | 2023-09-20 | 2023-09-20 | Concentrated spent acid joins in marriage sour device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220939130U (en) |
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2023
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