CN220696298U - Recovery and control device for byproduct ammonia gas generated in preparation of propylene carbon by urea method - Google Patents
Recovery and control device for byproduct ammonia gas generated in preparation of propylene carbon by urea method Download PDFInfo
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- CN220696298U CN220696298U CN202321776258.1U CN202321776258U CN220696298U CN 220696298 U CN220696298 U CN 220696298U CN 202321776258 U CN202321776258 U CN 202321776258U CN 220696298 U CN220696298 U CN 220696298U
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- ammonia
- liquid
- absorption tower
- collecting tank
- gas
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 153
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 239000004202 carbamide Substances 0.000 title claims abstract description 21
- 239000006227 byproduct Substances 0.000 title claims abstract description 18
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- 238000002360 preparation method Methods 0.000 title claims description 8
- JGNPSJMNGPUQIW-UHFFFAOYSA-N [C].CC=C Chemical compound [C].CC=C JGNPSJMNGPUQIW-UHFFFAOYSA-N 0.000 title claims description 5
- 238000010521 absorption reaction Methods 0.000 claims abstract description 94
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 239000000047 product Substances 0.000 claims abstract description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 4
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 4
- 239000007791 liquid phase Substances 0.000 claims description 25
- 239000000463 material Substances 0.000 claims description 17
- 230000001105 regulatory effect Effects 0.000 claims description 14
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000000605 extraction Methods 0.000 claims description 8
- 239000006260 foam Substances 0.000 claims description 7
- 230000001276 controlling effect Effects 0.000 claims description 5
- 239000007790 solid phase Substances 0.000 claims description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 11
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- DVARTQFDIMZBAA-UHFFFAOYSA-O ammonium nitrate Chemical compound [NH4+].[O-][N+]([O-])=O DVARTQFDIMZBAA-UHFFFAOYSA-O 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Recovery and controlling means of carbon by-product ammonia are made to urea method, include: the device comprises a demister (R1), an absorption tower (C1), a primary condenser (E1), a primary collecting tank (V1), an ammonia compressor (C2), a secondary condenser (E2), a liquid ammonia collecting pipe (V2), an absorption tower discharge pump (1), a liquid ammonia conveying pump (2) and an absorption liquid separator (S1). The device has the advantages of few equipment, simple operation, raw material saving and capability of producing high-quality liquid ammonia products.
Description
Technical Field
The utility model relates to the field of production of propylene carbonate by a urea method, in particular to a recovery and control device for byproduct ammonia gas generated in the process of preparing propylene carbonate by the urea method.
Background
Propylene carbonate is an important chemical product friendly to the environment, and the main production method for producing propylene carbonate in China is to react propylene oxide with carbon dioxide, so that the method has high raw material price, high risk, high-pressure reaction and high equipment investment, and the production cost for producing propylene carbonate is high. The urea method for producing propylene carbonate has the advantages of easily obtained raw materials, mild reaction conditions and low equipment investment, and ammonia gas which is an important chemical product can be produced as a byproduct in urea method production, so that the nitrogen fertilizer industry, the organic synthesis industry and the nitric acid, ammonium salt and sodium carbonate production are all indistinct. Ammonia is easily liquefied into liquid ammonia, and a large amount of heat is absorbed when the liquid ammonia is gasified, so that ammonia can also be used as a refrigerant. The ammonia is recovered into ammonia water after multi-stage circulating water washing by adopting low-temperature cooling spraying in China, and then the ammonia is purified by a distillation method to obtain the ammonia, and the ammonia is reused, so that more equipment is used and the investment is high.
Disclosure of Invention
The technical problem that the utility model solves lies in providing recovery and controlling means of urea method preparation propylene carbon by-product ammonia, the recovery and controlling means of this application provided urea method preparation propylene carbon by-product ammonia can effectually be with the ammonia purification recovery of by-product in the urea method preparation propylene carbonate technology, prepares liquid ammonia. In view of this, this application provides recovery and controlling means of urea method carbon-producing by-product ammonia, includes: the device comprises a foam remover, an absorption tower, a first-stage condenser, a first-stage collecting tank, an ammonia compressor, a second-stage condenser, a liquid ammonia collecting pipe, an absorption tower discharge pump, a liquid ammonia conveying pump, an absorption tower liquid level meter, an absorption tower discharge flowmeter, an absorption tower discharge regulating valve, a liquid ammonia collecting tank liquid level, a liquid ammonia extraction flowmeter, a liquid ammonia extraction regulating valve, an absorption tower top thermometer, an ammonia compressor pressure gauge, a liquid ammonia collecting tank thermometer, a liquid ammonia collecting tank pressure gauge and an absorption liquid separator; the device is characterized in that crude ammonia gas as a byproduct of the urea and propylene glycol reaction is connected with the bottom end of a demister, a gas phase discharge end at the top of the demister is connected with a feed end of an absorption tower, a gas phase discharge end at the top of the absorption tower is connected with a feed end of a first-stage condenser, a material at the discharge end of the first-stage condenser enters a first-stage collecting tank, the gas phase end of the first-stage collecting tank is connected with an air inlet end of an ammonia compressor, an air outlet end of the ammonia compressor is connected with an air inlet end of a second-stage condenser, a liquid phase end of the second-stage condenser and a liquid phase end of the ammonia compressor are connected with a feed end of a liquid ammonia collecting tank, and the liquid phase end of the liquid ammonia collecting tank is conveyed to a liquid ammonia product tank through a liquid ammonia conveying pump; the liquid phase discharging end at the bottom of the absorption tower is connected with the absorption liquid separator through a part of the absorption tower discharge pump, the liquid phase material separated by the absorption liquid separator is returned to the absorption tower, the solid phase material is packaged and sold, and a part of the liquid phase discharging end of the absorption tower discharge pump is converged with the liquid phase discharging end of the first-stage collecting tank and then enters the top of the absorption tower.
The inside of the demister is provided with a demisting net, so that liquid phase materials are prevented from being entrained into the absorption tower, and impurities in ammonia gas discharged from the top of the demister are prevented from being absorbed by the absorption tower.
The absorption liquid of absorption tower can absorb the impurity gas in the ammonia, when absorption liquid absorption impurity reaches saturation, need carry to flowing back jar, and the level gauge of absorption tower and absorption tower ejection of compact flowmeter, absorption tower ejection of compact governing valve have set up long-range DCS cascade chain control, can adjust the ejection of compact flow of absorption tower cauldron by oneself according to liquid level height, guarantee that the liquid level of absorption tower is steady, make the absorption liquid reach better absorption effect.
The outlet pressure of the ammonia gas compressor is controlled through frequency conversion, a pressure gauge is arranged at the top of the ammonia gas compressor, the pressure of the compressor is convenient to observe and adjust, and the operating pressure of the compressor is controlled to be 0.5-2.0MPa.
The utility model has the following advantages:
(1) Less equipment is used, so that investment is saved;
(2) The production device adopts DCS automatic control, so that the production operation is simplified;
(3) The absorption liquid used in the absorption tower can be recycled after being separated, so that the waste of materials is avoided;
(4) The quality of the produced liquid ammonia product is high, and the quality content is more than 99.5%.
Drawings
Fig. 1 is a schematic view of the apparatus of the present utility model.
Detailed Description
The utility model will now be further described with reference to the following examples, which are intended to illustrate, but not to limit, the utility model. The application provides a recovery and controlling means of urea method carbon by-product ammonia, include: the device comprises a foam remover, an absorption tower, a first-stage condenser, a first-stage collecting tank, an ammonia compressor, a second-stage condenser, a liquid ammonia collecting pipe, an absorption tower discharge pump, a liquid ammonia conveying pump, an absorption tower liquid level meter, an absorption tower discharge flowmeter, an absorption tower discharge regulating valve, a liquid ammonia collecting tank liquid level, a liquid ammonia extraction flowmeter, a liquid ammonia extraction regulating valve, an absorption tower top thermometer, an ammonia compressor pressure gauge, a liquid ammonia collecting tank thermometer, a liquid ammonia collecting tank pressure gauge and an absorption liquid separator (S1); the device is characterized in that crude ammonia gas as a byproduct of the urea and propylene glycol reaction is connected with the bottom end of a demister, a gas phase discharge end at the top of the demister is connected with a feed end of an absorption tower, a gas phase discharge end at the top of the absorption tower is connected with a feed end of a first-stage condenser, a material at the discharge end of the first-stage condenser enters a first-stage collecting tank, the gas phase end of the first-stage collecting tank is connected with an air inlet end of an ammonia compressor, an air outlet end of the ammonia compressor is connected with an air inlet end of a second-stage condenser, a liquid phase end of the second-stage condenser and a liquid phase end of the ammonia compressor are connected with a feed end of a liquid ammonia collecting tank, and the liquid phase end of the liquid ammonia collecting tank is conveyed to a liquid ammonia product tank through a liquid ammonia conveying pump; the liquid phase discharging end at the bottom of the absorption tower is connected with the absorption liquid separator through a part of the absorption tower discharge pump, the liquid phase material separated by the absorption liquid separator is returned to the absorption tower, the solid phase material is packaged and sold, and a part of the liquid phase discharging end of the absorption tower discharge pump is converged with the liquid phase discharging end of the first-stage collecting tank and then enters the top of the absorption tower.
The device brings crude ammonia generated by the reaction of urea and propylene glycol into an absorption tower with certain impurities carried by the crude ammonia through a demister, the temperature of the absorption tower is controlled at 80-120 ℃, and saturated solution of alkali metal is used as absorption liquid for absorbing gas phase impurities in the ammonia. The material at the bottom of the absorption tower is sprayed down through the discharge pump of the absorption tower, a part of the material is circulated and returned to the top of the absorption tower to be sprayed down, so that gas phase impurities in ammonia can be absorbed effectively, a part of the material is discharged to the separator of the absorption tower, the material liquid is separated, the separated liquid phase clear liquid is continuously returned to the absorption tower to be used continuously, the supplement amount of new absorption liquid can be reduced, the raw material investment is saved, the separated solid phase material is packaged for sale, the liquid level of the absorption tower is controlled to be 50%, cascade adjustment is carried out through the discharge flow meter of the absorption tower and the discharge flow regulating valve of the absorption tower, when the liquid level of the absorption tower is more than 50%, the valve position of the discharge flow regulating valve of the absorption tower is automatically regulated to be large, meanwhile, the flow on the discharge flow meter of the absorption tower is increased, when the liquid level of the absorption tower is more than 50%, the valve position of the discharge flow regulating valve of the absorption tower is more than normal, and when the liquid level of the absorption tower is less than 50%.
The ammonia which is primarily treated by the absorption tower possibly carries some small liquid beads, the ammonia enters a first-stage condenser for condensation, the condensation temperature of the first-stage condenser is controlled to be 50-70 ℃, the carried liquid beads are condensed, the ammonia enters a first-stage collecting tank, the condensed liquid phase returns to the absorption tower to serve as absorption liquid, gas phase at the top of the first-stage collecting tank enters an ammonia compressor for compression, the ammonia compressor utilizes a frequency converter to control the outlet pressure to be 0.5-2.0MPa, ammonia can be liquefied, the temperature of the liquid ammonia is controlled to be 70-120 ℃, uncondensed gas discharged by the ammonia compressor enters a second-stage condenser for condensation, the condensation temperature of the second-stage condenser is controlled to be 50-80 ℃, finally, the condensed liquid ammonia and the liquid ammonia discharged by the ammonia compressor are conveyed to a liquid ammonia collecting tank, the liquid level of the liquid ammonia collecting tank is controlled to be 50-100 ℃ under the pressure of 0.5-2.0MPa, and the liquid level of the liquid ammonia collecting tank is controlled to be 50% with a liquid ammonia extraction flowmeter and a liquid ammonia extraction regulating valve to be controlled by a stage DCS, so that the liquid level of the liquid ammonia collecting tank can be effectively regulated, and the liquid level of the liquid collecting tank is prevented from being too high or too low, and influencing normal production operation. The purity of the liquid ammonia produced by the device is more than 99.5 percent. The device meets the national standard of liquid ammonia, heating is not needed in the recovery section of ammonia gas, and the absorption liquid used can be recycled, so that the consumption of raw materials and the investment of public engineering are greatly saved.
The above embodiment is only one implementation form of the recovery and control device for the byproduct ammonia gas produced in the propylene preparation method by urea, and according to other variants of the scheme provided by the utility model, components or steps in the ammonia gas are added or reduced, or the ammonia gas recovery and control device is applied to the technical field similar to the utility model, and all belong to the protection scope of the utility model.
Claims (4)
1. Recovery and controlling means of carbon by-product ammonia are made to urea method, include: the device comprises a foam remover (R1), an absorption tower (C1), a primary condenser (E1), a primary collecting tank (V1), an ammonia compressor (C2), a secondary condenser (E2), a liquid ammonia collecting tank (V2), an absorption tower discharge pump (1), a liquid ammonia conveying pump (2), an absorption tower liquid level meter (L1), an absorption tower discharge flow meter (F1), an absorption tower discharge regulating valve (FV 1), a liquid ammonia collecting tank liquid level (L2), a liquid ammonia extraction flow meter (F2), a liquid ammonia extraction regulating valve (FV 2), an absorption tower top thermometer (T1), an ammonia compressor pressure gauge (P1), a liquid ammonia collecting tank thermometer (T2), a liquid ammonia collecting tank pressure gauge (P2) and an absorption liquid separator (S1); the device is characterized in that crude ammonia gas which is a byproduct of urea and propylene glycol reaction is connected with the bottom end of a foam remover (R1), the top gas phase discharge end of the foam remover (R1) is connected with the feed end of an absorption tower (C1), the top gas phase discharge end of the absorption tower (C1) is connected with the feed end of a primary condenser (E1), the material at the discharge end of the primary condenser enters a primary collecting tank (V1), the gas phase end of the primary collecting tank (V1) is connected with the gas inlet end of an ammonia compressor (C2), the gas outlet end of the ammonia compressor (C2) is connected with the gas inlet end of a secondary condenser (E2), the liquid phase end of the secondary condenser (E2) and the liquid phase end of the ammonia compressor (C2) are connected with the feed end of a liquid ammonia collecting tank (V2), and the liquid phase end of the liquid ammonia collecting tank (V2) is conveyed to a liquid ammonia product tank through a liquid ammonia conveying pump (2); the liquid phase discharging end at the bottom of the absorption tower (C1) is connected with the absorption liquid separator (S1) through a part of the absorption tower discharging pump (1), the liquid phase material separated by the absorption liquid separator (S1) returns to the absorption tower (C1), the solid phase material is packaged and sold, and a part of the liquid phase discharging end of the absorption tower discharging pump (1) is converged with the liquid phase discharging end of the first-stage collecting tank (V1) and then enters the top of the absorption tower (C1).
2. The recovery and control device for ammonia gas as a byproduct in the preparation of propylene by a urea method according to claim 1, wherein a foam removing net is arranged in the foam remover (R1) to prevent liquid phase materials from being entrained into the absorption tower (C1).
3. The recovery and control device for the ammonia gas byproduct produced in the propylene preparation method by the urea method according to claim 1 is characterized in that a liquid level meter (L1) of an absorption tower, an absorption tower discharge flow meter (F1) and an absorption tower discharge regulating valve (FV 1) are provided with remote DCS cascade linkage control, so that the discharge flow of the tower kettle of the absorption tower (C1) can be automatically regulated according to the liquid level height, and the liquid level stability of the absorption tower (C1) is ensured.
4. The recovery and control device for ammonia gas as a byproduct in the production of propylene carbon by urea process according to claim 1, wherein the ammonia gas compressor (C2) controls the outlet pressure by frequency conversion, and the operating pressure of the compressor is controlled to be 0.5-2.0MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321776258.1U CN220696298U (en) | 2023-07-07 | 2023-07-07 | Recovery and control device for byproduct ammonia gas generated in preparation of propylene carbon by urea method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321776258.1U CN220696298U (en) | 2023-07-07 | 2023-07-07 | Recovery and control device for byproduct ammonia gas generated in preparation of propylene carbon by urea method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220696298U true CN220696298U (en) | 2024-04-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321776258.1U Active CN220696298U (en) | 2023-07-07 | 2023-07-07 | Recovery and control device for byproduct ammonia gas generated in preparation of propylene carbon by urea method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220696298U (en) |
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2023
- 2023-07-07 CN CN202321776258.1U patent/CN220696298U/en active Active
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