Sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device
Through the use of MVR evaporation energy -saving devices in sodium acetate evaporation process, using heat recovery and recycling, the problem of high energy consumption in existing technologies has been solved, and significant energy consumption and production cost savings are achieved.
Patent Information
- Application Number
- CN202420559361.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-03-22
- Publication Date
- 2025-01-24
- Estimated Expiration
- 2034-03-22
AI Technical Summary
The existing sodium acetate trihydrate evaporation process has high energy consumption, resulting in excessive production costs.
The MVR evaporation energy -saving device is installed with sodium acetate. This device includes first -level pilom -mVR devices and secondary film reduction evaporation devices. It improves thermal efficiency through heat recovery and recycling.
By making full use of the latent heat and waste heat of the secondary steam, the energy consumption during the evaporation process is significantly reduced, and natural gas consumption and production costs are reduced.
Smart Images
Figure CN222384180U_ABST
Abstract
Description
Technical field:
[0001] The utility model belongs to the field of sodium acetate trihydrate evaporation technology, and specifically relates to a sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device. Technical background:
[0002] At present, the evaporation process used in the domestic production of sodium acetate trihydrate is in the form of a single kettle with oil bath or coil steam. This technology has the disadvantage of high energy consumption. In production, the liquid with a sodium acetate content of 20-32% after the ingredients are neutralized is pumped into a single kettle, and the liquid is stirred while passing steam in the kettle. The evaporated water vapor is discharged into the atmosphere through the coil, resulting in a large amount of heat waste and loss; when the sodium acetate content is evaporated to 42-46%, it is driven into a crystallizer, and after cooling, the slurry is driven into a centrifuge to separate sodium acetate trihydrate. This method requires 1.5 tons of steam to evaporate one ton of water, which is equivalent to 75-80m3 of natural gas. 3 , the production costs of enterprises are too high. Utility model content:
[0003] The utility model aims to overcome the shortcomings of the prior art and provide a sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device, which solves the technical problem of high energy consumption of the existing sodium acetate trihydrate evaporation process equipment.
[0004] In order to solve the above problems, the technical solution of the utility model is: a sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device, comprising a first-stage skid-mounted MVR device and a second-stage falling film evaporation device.
[0005] The first-stage skid-mounted MVR device includes a first-stage heat exchanger, a second-stage heat exchanger, a heat recovery heat exchanger, a compressor, a condensate recovery tank, a circulation pump, and a discharge pump; one raw water channel is connected to the raw water inlet of the first-stage heat exchanger through a pipeline, and another raw water channel is connected to the raw water inlet of the heat recovery heat exchanger through a pipeline; the raw water outlets of the first-stage heat exchanger and the heat recovery heat exchanger are connected to the raw water inlet of the second-stage heat exchanger through pipelines in parallel; the raw water outlet of the second-stage heat exchanger is connected to the upper circulation pipeline in the second-stage falling film evaporation device through a pipeline; the fresh steam is connected to the steam inlet of the second-stage heat exchanger through a pipeline, and the condensate outlet of the second-stage heat exchanger is connected to the condensate recovery tank through a pipeline; the drain outlet of the condensate recovery tank is connected to the condensate pump inlet through a pipeline, and the condensate pump outlet is connected to the condensate inlet of the first-stage heat exchanger through a pipeline The condensate outlet of the primary heat exchanger is connected to the condensate discharge through a pipeline and discharged to the plant area for collection and treatment; the inlet of the discharge pump is connected to the bottom of the separation chamber in the secondary falling film evaporation device through a pipeline, the outlet of the discharge pump is connected to the discharge inlet of the heat recovery heat exchanger through a pipeline, and the discharge outlet of the heat recovery heat exchanger is connected to the discharge collection through a pipeline and collected in the crystallization tank; the inlet of the compressor is connected to the top of the separation chamber in the secondary falling film evaporation device through a pipeline, and the outlet of the compressor is connected to the steam inlet of the shell and tube heat exchanger in the secondary falling film evaporation device through a pipeline; the inlet of the circulating pump is connected to the bottom connecting pipe of the separation chamber and the shell and tube heat exchanger in the secondary falling film evaporation device through a pipeline, and the outlet of the circulating pump is connected to the top feed port of the shell and tube heat exchanger in the secondary falling film evaporation device through a pipeline;
[0006] The two-stage falling film evaporation device includes a separation chamber and a shell-and-tube heat exchanger; the condensate outlet of the shell-and-tube heat exchanger is connected to the condensate recovery tank in the first-stage skid-mounted MVR device through a pipeline; the separation chamber and the shell-and-tube heat exchanger are connected in series through pipelines in the middle and bottom;
[0007] Optionally, the fresh steam is connected to the steam inlet of the shell-and-tube heat exchanger through a pipeline;
[0008] Optionally, the shell-and-tube heat exchanger is a one-way shell-and-tube or plate-type falling film evaporation heat exchanger;
[0009] Optionally, an automatic control device is also included, and the automatic control device is divided into automatic and manual states; the operating states are divided into: startup, liquid injection temperature rise, compressor frequency rise, concentration, material discharge, shutdown, and cleaning stages; the automatic control system is electrically connected to each temperature sensor, automatic regulating valve, switch valve, flow meter, flow switch, pressure sensor, and each water pump;
[0010] Optionally, the raw water enters the primary heat exchanger and the heat recovery heat exchanger through respective raw water pumps in two ways, and the raw water outlets of the primary heat exchanger and the heat recovery heat exchanger are connected in parallel through pipelines and then enter the raw water inlet of the secondary heat exchanger;
[0011] Optionally, the feed inlet of the shell-and-tube heat exchanger is at the top of the heat exchanger, and a dispersed spray device is provided for the internal feed;
[0012] Compared with the prior art, the beneficial effects of the utility model are as follows:
[0013] 1. In the evaporation energy-saving device of the utility model, the secondary steam coming out of the separation chamber is compressed by the compressor, the pressure and temperature of the secondary steam are increased, the thermal enthalpy is increased, and then it is transported to the shell and tube heat exchanger for use as heating steam. The circulating liquid in the separation chamber is maintained in a boiling state, and the heating steam itself is condensed into water. In this way, the secondary steam that was originally to be discarded is fully utilized, the latent heat is recovered, and the thermal efficiency is improved.
[0014] 2. In the evaporation energy-saving device of the utility model, the condensed water exchanges heat with the raw water through the primary heat exchanger, recovers the waste heat, and at the same time reduces the discharge temperature of the condensed water; the concentrated effluent liquid exchanges heat with the raw water through the heat recovery heat exchanger, recovers the waste heat, and at the same time reduces the heat required for subsequent cooling of the concentrated effluent liquid, saving energy consumption. Description of the drawings:
[0015] Figure 1 It is a structural schematic diagram of the evaporation energy-saving device in the embodiment;
[0016] Figure 2 Schematic diagram of the structure of the shell and tube heat exchanger in the embodiment: top feeding, with a spray device.
[0017] Reference numerals: primary skid-mounted MVR device (1), secondary falling film evaporation device (2), fresh steam (3), condensate collection area (4), concentrated effluent collection area (5), raw water (6), primary heat exchanger (8), heat recovery heat exchanger (9), secondary heat exchanger (10), No. 1 raw water pump (11), No. 2 raw water pump (12), condensate pump (13), circulation pump (14), discharge pump (15), compressor (16), condensate recovery tank (17), shell-and-tube heat exchanger (18), separation chamber (19); Specific implementation method:
[0018] The utility model is further described in detail below in conjunction with the accompanying drawings and embodiments.
[0019] Example
[0020] like Figure 1 , Figure 2As shown, this embodiment provides a sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device, comprising a first-stage skid-mounted MVR device (1) and a second-stage falling film evaporation device (2); the first-stage skid-mounted MVR device (1) comprises a first-stage heat exchanger (8), a second-stage heat exchanger (10), a heat recovery heat exchanger (9), a compressor (16), a condensate recovery tank (17), a circulation pump (14), and a discharge pump (15); raw water (6) is connected to the raw water inlet of the first-stage heat exchanger (8) through a pipeline, and another raw water (6) is connected to the raw water inlet of the heat recovery heat exchanger (9) through a pipeline; the first-stage heat exchanger (8) and the heat recovery heat exchanger (9) The raw water outlet is connected to the raw water inlet of the secondary heat exchanger (10) through a pipeline in parallel; the raw water outlet of the secondary heat exchanger (10) is connected to the upper circulation pipeline in the secondary falling film evaporation device (2) through a pipeline; the fresh steam (3) is connected to the steam inlet of the secondary heat exchanger (10) through a pipeline, and the condensate outlet of the secondary heat exchanger (10) is connected to the condensate recovery tank (17) through a pipeline; the drain outlet of the condensate recovery tank (17) is connected to the inlet of the condensate pump (13) through a pipeline, the outlet of the condensate pump (13) is connected to the condensate inlet of the primary heat exchanger (8) through a pipeline, and the condensate outlet of the primary heat exchanger (8) is connected to the condensate recovery tank (17) through a pipeline. The discharge (4) is connected to the external discharge and discharged to the plant area for collection and treatment; the inlet of the discharge pump (15) is connected to the bottom of the separation chamber (19) in the secondary falling film evaporation device (2) through a pipeline, the outlet of the discharge pump (15) is connected to the discharge inlet of the heat recovery heat exchanger (9) through a pipeline, the discharge outlet of the heat recovery heat exchanger (9) is connected to the discharge collection (5) through a pipeline, and the production area is collected to the crystallization tank; the inlet of the compressor (16) is connected to the top of the separation chamber (19) in the secondary falling film evaporation device (2) through a pipeline, and the outlet of the compressor (16) is connected to the steam inlet of the shell and tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline; The inlet of the circulation pump (14) is connected to the bottom connecting pipe of the separation chamber (19) and the shell-and-tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline, and the outlet of the circulation pump (14) is connected to the top feed port of the shell-and-tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline; the secondary falling film evaporation device (2) comprises a separation chamber (19) and a shell-and-tube heat exchanger (18); the condensate outlet of the shell-and-tube heat exchanger (18) is connected to the condensate recovery tank (17) in the primary skid-mounted MVR device (1) through a pipeline; the separation chamber (19) and the shell-and-tube heat exchanger (18) are connected in series at the middle and bottom through pipelines;
[0021] The above-mentioned shell-and-tube heat exchanger (18) and separation chamber (19) form a falling film evaporator, and the circulation of the solution in the falling film evaporator is mainly carried out by a circulation pump (14). The advantages of using a falling film circulation evaporator are: a large heat transfer coefficient and a low power of the circulation pump.
[0022] The secondary steam coming out of the separation chamber (19) is compressed by the compressor (16), and the pressure and temperature of the secondary steam are increased, and the thermal enthalpy is increased. The secondary steam is then transported to the shell-and-tube heat exchanger (18) to be used as heating steam, so that the circulating liquid in the shell-and-tube heat exchanger (18) is maintained in a boiling state, and the heating steam itself is condensed into water. In this way, the secondary steam that was originally to be discarded is fully utilized, the latent heat is recovered, and the thermal efficiency is improved.
[0023] The condensed water in the condensed water recovery tank (17) is heat exchanged with the raw water (6) through the primary heat exchanger (8), thereby recovering the waste heat and reducing the temperature of the condensed water collection area (4); the concentrated effluent liquid pumped out by the discharge pump (15) is heat exchanged with the raw water through the heat recovery heat exchanger (9), thereby recovering the waste heat and reducing the heat required for subsequent cooling of the concentrated effluent liquid collection area (5), thereby saving energy consumption.
[0024] exist Figure 1 In the process, the raw material in the raw water source (6) is sodium acetate, and the condensate collection area (4) is the condensate discharged to the outside of the boundary area and collected by the manufacturer. The fresh steam (3) comes from the outside of the boundary area, and the concentrated effluent collection area (5) is the concentrated effluent discharged to the subsequent crystallization tank.
[0025] The working principle is as follows: raw water (6) is transported to the primary heat exchanger (8) via the No. 1 raw water pump (11); another raw water (6) is transported to the heat recovery heat exchanger (9) via the No. 2 raw water pump (12); the raw water after heat exchange is mixed and input into the secondary heat exchanger (10), and after being heated by the fresh steam (3), it reaches a boiling state, and the condensed water enters the condensed water recovery tank (17), and the feed liquid enters the shell and tube heat exchanger (18) of the secondary falling film evaporator (2), is heated to maintain a boiling state, and enters the separation chamber (19) for flash evaporation and gas-liquid separation; the secondary steam passes through the pressure After the compressor (16) is pressurized and heated, it is input into the shell layer of the shell-and-tube heat exchanger (18) again to heat and heat the material in the tube layer. After the heat exchange, the condensed water is discharged into the condensed water recovery tank (17). The condensed water is input into the primary heat exchanger (8) through the condensed water pump (13) to exchange heat with the raw water (6), and then discharged to the condensed water collection area (4); when the concentration of the circulating liquid reaches the external discharge requirement, it is transported to the heat recovery heat exchanger (9) through the discharge pump (15) to exchange heat with the raw water, and then discharged to the concentrated external discharge collection area (5), that is, the concentrated external discharge liquid is discharged to the subsequent crystallization tank.
[0026] In the evaporation energy-saving device of this embodiment, the pipeline equipment is made of stainless steel.
[0027] In the evaporation energy-saving device of this embodiment, corresponding valves and other pipeline components are installed on the pipeline according to the working conditions.
[0028] The evaporation energy-saving device of this embodiment also includes an automatic control device, which is divided into automatic and manual states; the operating state is divided into: startup, liquid injection and temperature rise, compressor frequency increase, concentration, material discharge, shutdown, and cleaning stages. In the automatic operation state, except for the manual start button, the system executes the above steps in sequence. During the whole process, no personnel are required to be on duty on site, and one-button start is convenient to operate and use.
[0029] At present, in actual production, most manufacturers pump the liquid with a sodium acetate content of 20-32% after the ingredients are neutralized into a single kettle with a pump, stir it while passing steam in the kettle, evaporate it through a coil, and the evaporated water vapor is discharged into the atmosphere, resulting in a large amount of heat waste and loss; when the sodium acetate content is evaporated to 42-46%, it is pumped into a crystallizer, and after cooling, the crystal slurry is pumped into a centrifuge to separate sodium acetate trihydrate.
[0030] The advantages of the evaporation energy-saving device of this embodiment are:
[0031] 1. The evaporation equipment is compact and occupies a small area. The space required is 1 / 3 of the original area. The equipment does not require on-site construction and installation, and the cooling system can be omitted. For existing production enterprises that need to expand evaporation equipment but have insufficient steam and water supply capacity and insufficient space, it can save investment and achieve better energy-saving effects.
[0032] 2. According to the current market price of 4 yuan / m 3 Natural gas, 75m3 per ton of steam 3 Calculated by natural gas, the traditional evaporation equipment for sodium acetate trihydrate production requires 1.5 tons of steam to evaporate one ton of water, which requires 75m 3 ×4 yuan / m 3 ×1.5t=450 yuan. The evaporation energy-saving device of this embodiment requires 0.26t of fresh steam to evaporate one ton of water, and the production cost is 0.26t×75m 3 ×4 yuan / m 3 =78 yuan, which saves the company's production costs to a great extent.
[0033] The implementation modes of the present invention are described in detail above in conjunction with the accompanying drawings, but the present invention is not limited to the above implementation modes. The implementation modes can still be changed within the knowledge scope of ordinary technicians in the field. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.
Claims
1. A sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device, characterized in that: It comprises a first-stage skid-mounted MVR device (1) and a second-stage falling film evaporation device (2); The first-stage skid-mounted MVR device (1) comprises a first-stage heat exchanger (8), a second-stage heat exchanger (10), a heat recovery heat exchanger (9), a compressor (16), a condensate recovery tank (17), a circulation pump (14), and a discharge pump (15); raw water (6) is connected to the raw water inlet of the first-stage heat exchanger (8) through a pipeline, and another raw water (6) is connected to the raw water inlet of the heat recovery heat exchanger (9) through a pipeline; the raw water outlets of the first-stage heat exchanger (8) and the heat recovery heat exchanger (9) are connected in parallel through pipelines to the second-stage heat exchanger (17). The raw water inlet of the heat exchanger (10) is connected; the raw water outlet of the secondary heat exchanger (10) is connected to the upper circulation pipeline in the secondary falling film evaporation device (2) through a pipeline; the fresh steam (3) is connected to the steam inlet of the secondary heat exchanger (10) through a pipeline, and the condensate outlet of the secondary heat exchanger (10) is connected to the condensate recovery tank (17) through a pipeline; the drain outlet of the condensate recovery tank (17) is connected to the inlet of the condensate pump (13) through a pipeline, and the outlet of the condensate pump (13) is connected to the cooling water of the primary heat exchanger (8) through a pipeline. The condensate inlet is connected, and the condensate outlet of the primary heat exchanger (8) is connected to the condensate discharge (4) through a pipeline and discharged to the plant area for collection and treatment; the inlet of the discharge pump (15) is connected to the bottom of the separation chamber (19) in the secondary falling film evaporation device (2) through a pipeline, and the outlet of the discharge pump (15) is connected to the hot material inlet of the heat recovery heat exchanger (9) through a pipeline, and the hot material outlet of the heat recovery heat exchanger (9) is connected to the discharge collection (5) through a pipeline, and the production area collects the hot material in the crystallization tank; the inlet of the compressor (16) is connected to the bottom of the separation chamber (19) in the secondary falling film evaporation device (2) through a pipeline, and the outlet of the discharge pump (15) is connected to the hot material inlet of the heat recovery heat exchanger (9) through a pipeline, and the hot material outlet of the heat recovery heat exchanger (9) is connected to the discharge collection (5) through a pipeline, and the hot material in the production area is collected to the crystallization tank; the inlet of the compressor (16) is connected to the bottom of the separation chamber (19) in the secondary falling film evaporation device (2) through a pipeline, and the hot material inlet ... The compressor (16) is connected to the top of the separation chamber (19) in the secondary falling film evaporation device (2); the outlet of the compressor (16) is connected to the steam inlet of the shell-and-tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline; the inlet of the circulation pump (14) is connected to the bottom connecting pipe of the separation chamber (19) and the shell-and-tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline; the outlet of the circulation pump (14) is connected to the top feed port of the shell-and-tube heat exchanger (18) in the secondary falling film evaporation device (2) through a pipeline; The two-stage falling film evaporation device (2) comprises a separation chamber (19) and a shell-and-tube heat exchanger (18); the condensate outlet of the shell-and-tube heat exchanger (18) is connected to a condensate recovery tank (17) in a first-stage skid-mounted MVR device (1) via a pipeline; the separation chamber (19) and the shell-and-tube heat exchanger (18) are connected in series via pipelines at the middle and bottom.
2. The sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device according to claim 1, characterized in that: The fresh steam (3) is connected to the steam inlet of the shell-and-tube heat exchanger (18) through a pipeline.
3. The sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device according to claim 1, characterized in that: The shell and tube heat exchanger (18) is a falling film evaporator.
4. The sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device according to claim 1, characterized in that: It includes an automatic control device, which is divided into automatic and manual states; the operating states are divided into: startup, liquid injection and temperature rise, compressor frequency increase, concentration, discharging, shutdown, and cleaning stages; the automatic control system is electrically connected to each temperature sensor, automatic regulating valve, switch valve, flow meter, flow switch, pressure sensor, and each water pump.
5. The sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device according to claim 1, characterized in that: The raw water (6) is pumped into the primary heat exchanger (8) through the first raw water pump (11), and another stream of raw water (6) is pumped into the heat recovery heat exchanger (9) through the second raw water pump (12); the raw water outlets of the primary heat exchanger (8) and the heat recovery heat exchanger (9) are connected in parallel through pipelines and then enter the raw water inlet of the secondary heat exchanger (10).
6. The sodium acetate trihydrate skid-mounted MVR evaporation energy-saving device according to claim 1, characterized in that: The feed inlet of the shell-and-tube heat exchanger (18) is at the top of the heat exchanger, and a dispersed spray device is provided inside the feed.